Catalyst for hydrogenation of carbonyl compound and alcohol production method

ABSTRACT

Provided is a catalyst including a metal component including a first component that, is rhenium and one or more second components selected from the group consisting of silicon, gallium, germanium, and indium and a carrier on which the metal component is supported, the carrier including an oxide of a metal belonging to Group 4 of the periodic table. Also provided is an alcohol production method in which a carbonyl compound is treated using the above catalyst, it is possible to produce an alcohol by a hydrogenation reaction of a carbonyl compound with high selectivity and high efficiency while reducing 3ide reactions.

TECHNICAL FIELD

The present invention relates specifically to a catalyst useful as acatalyst for hydrogenation of a carbonyl compound and an alcoholproduction method in which a carbonyl compound is hydrogenated using thecatalyst.

BACKGROUND ART

Methods in which a carbonyl compound is hydrogenated to form acorresponding alcohol have long been known. For example, a commonalcohol production method from an organic carboxylic acid is to esterifya carboxylic acid with a lower alcohol and subsequently performreduction using an Adkins catalyst (copper chromite catalyst).

However, the production of an alcohol with a copper catalyst, which iscommonly conducted under a severe condition such as a hydrogen pressureof 200 atmospheres or more, is an uneconomical process that consumes alarge amount of energy for producing an alcohol and introduces variousfacility restrictions. Furthermore, since a copper catalyst is notcapable of directly reducing an organic carboxylic acid, a carboxylicacid needs to be converted into a carboxylic acid ester before areduction treatment is performed. Therefore, multistage reactionprocesses need to be conducted in order to produce an intended alcohol.This increases the complexity of the process.

Moreover, in the case where the above production method is used, itbecomes considerably difficult to selectively produce ahydroxycarboxylic acid using, for example, a polyvalent carboxylic acidas a raw material by converting a part of the carboxylic acid functionalgroup3 into alcohol functional groups.

In contrast, a method in which a carboxylic acid is directlyhydrogenated (reduced) in one stage and a corresponding alcohol isproduced with high selectivity is an economically advantageous process.Even in the case where a polyvalent carboxylic acid is used as a rawmaterial, it is possible to selectively produce a correspondinghydroxycarboxylic acid by appropriately controlling the reactionconditions.

There have been proposed various metal-supporting catalysts that includea noble metal belonging to Groups 3 to 10 of the periodic table as acatalytic activity component, for use in such a process. Examples of themetal-supporting catalysts include a catalyst produced by attachingpalladium and rhenium to a carrier and subsequently performing areduction treatment with hydrogen or the like (e.g., PTL 1 and NPL 1)and a catalyst produced by attaching ruthenium and tin to a carrier andsubsequently performing a reduction treatment with hydrogen or the like(e.g., PTLs 2 and 3).

The above catalysts are suitable catalysts that have a high reactionactivity and high reaction selectivity in the reduction of a carboxylicacid and/or a carboxylic acid eater. There has also beer, proposed ahydrogenation reaction of a particular carboxylic acid In which a cobaltcatalyst that includes lanthanum and palladium, which is an example ofthe above-described catalysts, is used (e.g., PTL 4).

On the other hand, there have also been proposed catalysts that do notinclude any of the expensive noble metals belonging to Groups 8 to 10 ofthe periodic table. For example, a catalyst including rhenium thatserves as a catalytic component has been reported since a long time ago(e.g., NPL 2). There has also been proposed a tin-containing rheniumcatalyst for use in a hydrogenation reaction of a particular carboxylicacid (e.g., PTL 5). Recently, there has been reported a method forselectively producing an intended alcohol under further mild conditions.In the production method, a metal-supporting catalyst including rheniumthat serves as a catalytic activity component is used (e.g., NPLs 3 and4).

However, since catalysts including rhenium that serves as a catalyticactivity component have lower catalytic activity than catalystsincluding a noble metal, it is common to use, as a supported metal,rhenium in combination with a noble metal belonging to Groups 8 to 10 ofthe periodic table or to add cobalt, which belongs to Group 9 of theperiodic table, to a carrier (e.g., PTLs 6, 7, 8, and 9 and NPL 5).

PTL 1: Japanese Unexamined Patent Application Publication No. 63-218636

PTL 2: Japanese Unexamined Patent Application Publication No.2000-007596

PTL 3: Japanese Unexamined Patent Application Publication No.2001-157841

PTL 4: Japanese Unexamined Patent Application Publication No. 63-301845

PTL 5: Japanese Unexamined Patent Application Publication No. 4-99753

PTL 6: Japanese Unexamined Patent Application Publication No. 6-116182

PTL 7: Japanese Unexamined Patent Application Publication (Translationof PCT Application) No. 2002-501817

PTL 8: Japanese Unexamined Patent Application Publication (Translationof PCT Application) No. 2016-500697

PTL 9: Japanese Unexamined Patent Application Publication No. 7-119187

NFL 1: Topics in Catalysis 55 (2012) 466-473

NPL 2: Journal of Organic Chemistry 24 (1959) 1847-1854

NPL 3: Journal of Catalysis 328 (2015) 197-207

NPL 4: Chemistry A European Journal 23 (2017) 1001-1006

NPL 5: ACS Catalysis 5 (2015) 7034-7047

SUMMARY OF INVENTION Technical Problem

A catalyst including a noble metal belonging to Groups 6 to 10 of theperiodic table which serves as a catalytic activity component, which isproduced using an expensive noble metal, increases the costs ofproduction of a catalyst. In addition, such a catalyst typically causesside reactions, such as a degradation reaction that involvesdecarboxylation, a defunctionalization reaction associated withdehydration and hydrogenation of the reaction product, and anesterification reaction of a carboxylic acid used as a raw material withan alcohol produced. Thus, it is necessary to reduce the above sidereactions.

For example, as for a palladium metal-supporting catalyst containingrhenium, the addition of rhenium increases the rate of catalyticreaction in which succinic acid is converted into the hydride ofsuccinic acid, that is, butanediol, as described in NPL 1. However, theabove-described side reactions also occur, which reduce the productivityof the reaction product, and increase the purification costs. Inaddition, the catalytic activity of such a catalyst is still at aninsufficient level.

As for the catalysts that include a catalytic component, such as tin, inaddition to a noble metal belonging to Groups 8 to 10 of the periodictable as proposed in PTLs 2 and 3, the addition of tin or the likeincreases reaction selectivity. However, the addition of such catalyticcomponents may disadvantageously reduce catalytic activity. This resultsin a necessity to further use a large amount of expensive noble metal,such as platinum, and increases the costs of production or a catalyst.

The catalyst including rhenium that serves as a principal catalyticactivity component allows a highly economical process to be realized inthe sense that the catalyst does not include any expensive noble metal.However, such catalysts typically have lower activity than catalyststhat include a noble metal. Moreover, an esterification reaction of acarboxylic acid used as a raw material with an alcohol produced islikely to occur due to high Lewis acidity of rhenium and, particularlyat a later stage of the reaction, a defunctionalization reaction maysignificantly occur due to the dehydration and hydrogenation of thealcohol produced. This significantly reduces the selectivity of thealcohol that is t.c be produced.

An object of the present Invention is to provide a highly economicalalcohol production method that enables an intended alcohol to beproduced at a high yield with high selectivity by the hydrogenationreaction of a carbonyl compound while reducing the above-describedvarious side reactions to a sufficient degree.

Another object of the present invention is to provide a high-activitymetal-supporting catalyst including rhenium which enables an intendedalcohol to be produced at a high yield with high selectivity by thehydrogenation reaction of a carbonyl compound while reducing the sidereactions and a method for producing such a metal-supporting catalyst.

Solution to Problem

The inventors of the present invention found that the above issue3 maybe addressed by using a catalyst produced by attaching rhenium and aspecific second component to a carrier when an alcohol is produced bythe hydrogenation reaction of a carbonyl compound and consequently madethe present invention.

The summary of the first aspect of the present invention (hereinafter,referred to as “first invention”) is as follows.

-   [1-1] An alcohol production method in which an alcohol is produced    from a carbonyl compound, the method comprising producing an alcohol    by using a catalyst, the catalyst including a metal component    including a first component that is rhenium and one or more second    components selected from the group consisting of silicon, gallium,    germanium, and indium and a carrier or which the metal component is    supported, the carrier including an oxide of a metal belonging to    Group 4 of the periodic table.-   [1-2] The alcohol production method according to [1-1], wherein the    mass ratio of elements that are the second components included in    the catalyst to the rhenium element included in the catalyst is 0.1    or more and 10 or less.-   [1-3] The alcohol production method according to [1-1] or [1-2],    wherein the oxide of a metal belonging to Group 4 of the periodic    table, the oxide being included in the catalyst, includes titanium    oxide and/or zirconium oxide.-   [1-4] The alcohol production method according to any one of [1-1] to    [1-3], wherein the catalyst is a catalyst prepared by a method    including a step in which the metal component is attached to a    carrier including a sulfate ion.-   [1-5] The alcohol production method according to [1-4], wherein the    sulfate ion content in the carrier is 0.01% by mass or more and 10%    by mass or less of the mass of the carrier.-   [1-6] The alcohol production method according to any one of [1-1] to    [1-5], wherein the sulfate ion content in the catalyst is 0.01% by    mass or more and 10% by mass or less of the mass of the catalyst.-   [1-7] A catalyst comprising a metal component including a first    component that is rhenium and one or more second components selected    from the group consisting of silicon, gallium, germanium, and    indium, and a carrier on which the metal component is supported, the    carrier including an oxide of a metal belonging to Group 4 of the    periodic table.-   [1-8] The catalyst according to [1-7], wherein the mass ratio of    elements that are the second components to the rhenium element is    0.1 or more and 10 or less.-   [1-9] The catalyst according to [1-7] or [1-8], wherein the oxide of    a metal belonging to Group 4 of the periodic table includes titanium    oxide and/or zirconium oxide.-   [1-10] The catalyst according to any one of [1-7] to [1-9], wherein    the sulfate ion content in the catalyst is 0.01% by mass or more and    10% by mass or less of the mass of the catalyst.-   [1-11] The catalyst according to any one of [1-7] to [1-10], the    catalyst being a catalyst used for hydrogenation of a carbonyl    compound.

The summary of the second aspect of the present invention (hereinafter,referred to as “second invention”) is as follows.

-   [2-1] An alcohol production method in which an alcohol is produced    from a carbonyl compound, the method comprising producing an alcohol    by using a catalyst, the catalyst including a metal component    including a first component that is rhenium and one or more second    components selected from the group consisting of silicon, gallium,    germanium, and indium and a carrier on which the metal component is    supported, the mass ratio of elements that are the second components    to the rhenium element being 0.1 or more and 10 or less.-   [2-2] The alcohol production method according to [2-1], wherein the    second components of the catalyst include germanium.-   [2-3] The alcohol production method according to [2-1] or [2-2],    wherein the mass ratio of a metallic element belonging to Groups 3    to 10 of the periodic table to the rhenium element included in the    catalyst, the metallic element being other than iron or nickel, is    less than 0.2.-   [2-4] The alcohol production method according to [2-3], wherein the    metallic element belonging to Groups 3 to 10 of the periodic table,    the metallic element being included in the catalyst, the metallic    element being other than iron or nickel, includes ruthenium.-   [2-5] The alcohol production method according to any one of [2-1] to    [2-4], wherein the carrier is a carbonaceous carrier or a carrier    including an oxide of n metal belonging to Group 4 of the periodic    table.-   [2-6] The alcohol production method according to any one of [2-1] to    [2-5], wherein the catalyst is a catalyst prepared by a method    including a step in which the metal component is attached to a    carrier including a sulfate ion.-   [2-7] The alcohol production method according to [2-6], wherein the    sulfate ion content in the carrier is 0.01% by mass or more and 10%    by mass or less of the mass of the carrier.-   [2-8] The alcohol production method according to any one of [2-1] to    [2-7], wherein the sulfate ion content in the catalyst is 0.01% by    mass or more and 10% by mass or less of the mass of the catalyst.-   [2-9] A catalyst comprising a metal component including a first    component that is rhenium and one or more second components selected    from the group consisting of silicon, gallium, germanium, and indium    and a carrier on which the metal component is supported, the mass    ratio of elements that are the second components to the rhenium    element being 0.1 or more and 10 or less.-   [2-10] The catalyst according to [2-9], wherein the second    components include germanium.-   [2-11] The catalyst according to [2-9] or [2-10], wherein the mass    ratio of a metallic element belonging to Groups 3 to 10 of the    periodic table to the amount of the rhenium element, the metallic    element being other than iron or nickel, is less than 0.2.-   [2-12] The catalyst according to [2-13], wherein the metallic    element belonging to Groups 8 to 10 of the periodic table, the    metallic clement being other than iron or nickel, includes    ruthenium.-   [2-13] The catalyst according to any one of [2-9] to [2-12], wherein    the carrier is a carbonaceous carrier or a carrier including an    oxide of a metal belonging to Group 4 of the periodic table.-   [2-14] The catalyst according to any one of [2-9] to [2-13], wherein    the sulfate ion content in the catalyst is 0.01% by mass or mere and    10% by mass or less.-   [2-15] The catalyst according to any one of [2-9] to [2-14], the    catalyst being a catalyst used for hydrogenation of a carbonyl    compound.-   [2-16] A method for producing a catalyst, the method comprising    attaching a metal component including at least a first component    that is rhenium and one or more second components selected from the    croup consisting of silicon, gallium, germanium, and indium to a    carrier including a sulfate ion, the content of the sulfate ion in    the carrier being 0.01% by mass or more and 10% by mass or less of    the mass of the carrier.

Advantageous Effects of Invention

According to the first invention, there is provided an alcoholproduction method in which a carbonyl compound is reduced into analcohol with high activity and high selectivity by using a reductioncatalyst including rhenium that serves as a catalytic activitycomponent, the catalyst further including one or more catalytic additivecomponents selected from the group consisting of silicon, gallium,germanium, and indium and a carrier including an oxide of a metalbelonging to Group 4 of the periodic table, the catalytic additivecomponents being supported on the carrier. Also provided is the catalystuseful for producing an alcohol. Note that the term “periodic table”used herein refers to the long form of periodic table (Nomenclature ofInorganic Chemistry IUPAC recommendations 2005).

The catalyst according to the first invention enables an increase incatalytic activity, which has been an issue for rhenium catalysts, to beachieved substantially without using noble metals belonging to Groups 8to 10 of the periodic table. The catalyst according to the firstInvention also makes it possible to produce an alcohol from a carbonylcompound while reducing side reactions, such as an esterificationreaction of a carboxylic acid used as a raw material with an alcoholproduced and a defunctionalization reaction due to the dehydration andhydrogenation of the alcohol produced, which significantly occursparticularly at a later stage of the reaction, to a high degree. Itbecomes also possible to, in the case where a polyvalent carboxylic acid13 used as a raw material, produce a hydroxycarboxylic acid with highselectivity by converting a part of the carboxylic acid functionalgroups into alcohol functional groups.

According to the second invention, there is provided an alcoholproduction method in which a carbonyl compound is reduced into analcohol with high activity and high selectivity by using a reductioncatalyst including rhenium that serves as a catalytic activitycomponent, the catalyst further including one or more catalytic additivecomponents selected from the group consisting of silicon, gallium,germanium, and indium at a predetermined elemental mass ratio and acarrier, the catalytic additive components being supported on thecarrier. Also provided is the catalyst useful for producing an alcohol.

The catalyst according to the second invention enables an increase incatalytic activity, which has been an issue for rhenium catalysts, to beachieved substantially without using noble metals belonging to Groups 8to 10 of the periodic table. The catalyst according to the secondinvention also makes it possible to produce an alcohol from a carbonylcompound while reducing side reactions, such as the esterificationreaction of a carboxylic acid used as a raw material with an alcoholproduced and a defunctionalization reaction due to the dehydration andhydrogenation of the alcohol produced, which significantly occursparticularly at a later stage of the reaction, to a high degree. Itbecomes also possible to, in the ease where a polyvalent carboxylic acidis used as a raw material, produce a hydroxycarboxylic acid with highselectivity by converting a part of the carboxylic acid functionalgroups into alcohol functional groups.

DESCRIPTION OF EMBODIMENTS

Embodiments of the present, invention are described below in detail. Theelements described below are merely an example (typical example) of anaspect of the present invention. The present invention is not limited bythe description and may be modified within the scope of the presentinvention.

In the present invention, catalytic components supported on a carrier(e.g., rhenium; one or more elements selected from the group consistingof silicon, gallium, germanium, and indium; and optional metal elementsbelonging to Groups 8 to 10 of the periodic table, such as ruthenium)may be referred to collectively as “metal components”.

A material produced by attaching the metal components to a carrier maybe referred to as “metal-supporting material”.

A catalyst, produced by reducing the metal-supporting material may bereferred to as “metal-supporting catalyst”.

In the present invention, the metal components supported on the carrierare the same as the metal components included in the catalyst.

The content of the supported metal in the catalyst can be determined bypublicly known analysis methods, such as inductively coupled plasma massspectrometry (ICP-MS), inductively coupled plasma atomic emissionspectrometry (ICP-AES), atomic absorption spectrometry (AAS), and X-rayfluorescence analysis (XRK). In the case where ICP-MS, ICP-AES, and AASare used, the sample is formed into a solution in a pretreatmentconducted in combination with the analysis. The type of the analysismethod used is not limited since an appropriate analysis method varieswith the element subjected to the quantitative analysis, theconcentration of the element, and the accuracy required for theanalysis. In the present invention, the quantitative analysis of thesupported metal included in the catalyst is conducted using inductivelycoupled plasma atomic emission spectrometry, atomic absorptionspectrometry, or both inductively coupled plasma atomic emissionspectrometry and atomic absorption spectrometry in order to determinethe metal content in the catalyst.

The mass ratio between the metal components supported on the carrier iscalculated on the basis of the metal components included in the catalystas in the description of the method for determining the content of thesupported metal in the catalyst. The mass ratio between the rheniumelement an a the second component element can be determined usingpublicly known analysis methods, such as inductively coupled plasma massspectrometry (ICP-MS), inductively coupled plasma atomic emissionspectrometry (ICP-AES), atomic absorption spectrometry and X-rayfluorescence analysis (XRF), as in the description of the method fordetermining the content, of the supported metal in the catalyst.

In the present invention “% by weight” and “% by mass” are synonymouswith each other, and “element” and “atom” are synonymous with eachother.

The catalyst according to the present invention can be suitably used asa hydrogenation catalyst when an alcohol is produced from a carbonylcompound. In the present invention, a carbonyl compound is defined as acompound that includes a carbon-oxygen double bond (C═O), and

An alcohol is defined as a compound produced by converting the carbonylcompound into an alcohol functional group (OH).

Therefore, in the present invention, in the case where a carbonylcompound used as a raw material includes a plurality of carbon-oxygendouble bonds, a compound produced by converting at least one of thecarbon-oxygen double bonds of the carbonyl compound into an alcoholfunctional group is defined as an alcohol.

Catalyst According to First Invention

A catalyst according to the first invention (hereinafter, may bereferred to simply as “first catalyst”) is a metal-supporting catalystthat includes a metal component and a carrier on which the metalcomponent is supported. Specifically, the metal components including afirst component that is rhenium arid one or more second componentsselected from the group consisting of silicon, gallium, germanium, andindium are supported on a carrier including an oxide of a metalbelonging to Group 4 of the periodic cable.

The first catalyst is normally produced by reducing a metal-supportingmaterial on which the metal component is supported with a reducing gasand then performing an oxidative stabilization treatment as needed.

<Metal Component>

The metal component supported on the metal-supporting catalyst accordingto the first invention includes a first component that is rhenium andone or more second components selected from the group consisting ofsilicon, gallium, germanium, and indium. Among these, the secondcomponents used in combination with rhenium are preferably one or moreelements selected from the group consisting of silicon, germanium, andindium, are more preferably one or more elements that include indiumend/or germanium, are further preferably one or more elements thatinclude germanium, and are particularly preferably germanium.

As for the ratio between the amounts of the above essential componentssupported on the catalyst, the lower limit for the mass ratio of thesecond component elements that are one or mere elements selected fromthe group consisting of silicon, gallium, germanium, and indium to therhenium element is preferably 0.1 or more and is more preferably 0.5 ormore, and the upper limit for the above mass ratio is preferably 10 orless, is more preferably 5 or less, is further preferably 3 or less, isparticularly preferably 2 or less, and is most preferably 1 or less.

Appropriately selecting the types of the second components used incombination with rhenium and/or the proportion of the second componentssupported on the carrier increases the catalytic activity in ahydrogenation reaction of a carbonyl compound and makes it possible toproduce an alcohol while reducing side reactions, such as theesterification reaction of a carboxylic acid used as a raw material withan alcohol produced and a defunctionalization reaction due to thedehydration and hydrogenation of the alcohol produced, whichsignificantly occurs particularly at a later stage of the reaction, to ahigh degree. Using the above metal components in combination with oneanother enables the first catalyst to be handled in the air atmosphere.This increases ease of operation, such as transportation and storage ofthe catalyst and introduction cf the catalyst to a reactor in theproduction of an alcohol.

Using the above metal components in combination with one another enablesan increase in catalytic activity and an increase in reactionselectivity, which have been Considered contradictory, to be bothachieved presumably for the following reasons: the addition of thesecond components enables the electronic state of rhenium, which is acatalytic activity component of the hydrogenation catalyst, to becontrolled to be in a state suitable for a reduction reaction of acarbonyl functional group; the adsorptivity of reactive substrates ontothe surface of the catalyst is enhanced due to the affinity of thereactive substrates tor the second components; and the orientation ofadsorption of the reactive substrates on the surface of the catalyst iscontrolled at a high degree.

Although the amount of rhenium supported on the first catalyst is notlimited, the mass ratio of the rhenium element, to the total mass of themetal-supporting catalyst is normally 0.5% by mass or more, ispreferably 1% by mass or more, is more preferably 3% by mass or snore,is normally 20% by mass or less, is preferably 10% by mass or less, andis more preferably 8% by mass or less. When the amount of rheniumsupported on the catalyst is limited to be equal to or more than thelower limit, sufficiently high catalytic activity can be achieved. Thisprevents, for example, an increase in the volume of the reactor used.When the amount of rhenium supported on the catalyst is limited to beequal to or less than the upper limit, an increase in the cost of thecatalyst can be limited, furthermore, in such a case, coagulation ofrhenium supported on the catalyst can be reduced. This reduces the sidereactions, such as a degradation reaction involved by decarboxylation, adefunctionalization reaction associated with dehydration andhydrogenation of the reaction product, and an esterifications reactionof a carboxylic acid used as a raw material with an alcohol produced,due to high Lewis acidity of rhenium. As a result, reaction selectivitycan be further increased.

The first catalyst may further include, as needed, a third componentthat is a metal component other than the above metal components (i.e.,rhenium and the second components) and that does not adversely affectthe reactions conducted using the. first catalyst, such as a reductionreaction. Examples of the other metal component include metal componentsbelonging to Groups 3 to 10 of the periodic table except iron andnickel. Examples thereof include at least one metal selected from thegroup consisting of ruthenium, cobalt, rhodium, iridium, palladium, andplatinum which are capable of catalyzing hydrogenation.

Metals, such as iron and nickel, may elute and enter the catalyst when ametal reaction container made of SS, SUS, or the like becomes corrodedin the preparation oil the catalyst and/or the reaction. In the firstinvention, in the case where the eluted metal is precipitated on thecatalyst and included in the catalyst, the metal is not defined as ametal component of the first catalyst. In the case of elution from areaction container made of SUS, in addition to iron, the followingmetals may be detected in the catalyst in trace amounts at specificcontents depending on the material used.

For example, when metals enter from SUS201, nickel, chromium, andmanganese may foe detected in addition to iron at specific contents.When metals enter from SUS202, nickel chromium, and manganese may foedetected in addition to iron at specific contents. When metals enterfrom SUS301, nickel and chromium may be detected in addition to iron atspecific contents. When metals enter from SUS302, nickel and chromiummay be detected in addition to iron at specific contents. When metalsenter from SUS303, nickel, chromium, and molybdenum may be detected inaddition to iron at specific contents. When metals enter from SUS304,nickel and chromium may be detected in addition to iron at specificcontents. When metals enter from SUS305, nickel and chromium may bedetected in addition to iron at specific contents. When metals enterfrom SUS316, nickel, chromium, and molybdenum may be detected inaddition to iron at specific contents. When metals enter from SUS317,nickel, chromium, and molybdenum may be detected in addition to iron atspecific contents. When metals enter from SUS329J1, nickel, chromium,and molybdenum may be detected in addition to iron at specific contents.When metals enter from SUS403, chromium may be detected in addition toiron at a specific content. When metals enter from SUS405, chromium andaluminum may be detected in addition to iron at specific contents. Whenmetals enter from SUS420, chromium may be detected in addition to ironat a specific content. When metals enter from SUS430, chromium may bedetected in addition to iron at a specific content. When metals enterfrom 8US430LX, chromium, titanium, or niobium may be detected inaddition to iron at a specific content. When metals enter from SUS630,nickel, chromium, copper, and niobium may be detected in addition toiron at specific contents.

Examples of the metal component that belongs to a group other thanGroups 8 to 10 of the periodic table include at least one metal selectedfrom the group consisting of silver, gold, molybdenum, tungsten,aluminum, and boron.

Among the above third components, at least one metal selected fromruthenium, cobalt, rhodium, iridium, palladium, platinum, gold,molybdenum, and tungsten is preferable; at least one metal selected fromruthenium, cobalt, rhodium, iridium, palladium, platinum, molybdenum,arid tungsten is more preferable; at least one metal selected fromruthenium, iridium, palladium, and platinum is particularly preferable;and ruthenium is most preferable.

In the case where the third component is selected from rare andexpensive metals belonging to Groups 8 to 10 of the periodic tableexcept iron and nickel, the elemental mass ratio of the third componentincluded in the first catalyst to the rhenium element is normally lessthan 0.2, is preferably 0.15 or less, is more preferably 0.1 or less, isfurther preferably less than 0.1, and is most preferably 0 in order toincrease reaction selectivity and economical efficiency in terms of thecosts for producing the catalyst. That is, it is preferable that thefirst catalyst substantially do not include any of the rare andexpensive metals belonging to Groups 8 to 10 of the periodic table otherthan iron or nickel.

In the case where the third component is selected from metals other thanthe noble metals belonging to Groups 8 to 10 of the periodic table, theelemental mass ratio of the third component to the rhenium element isnormally 10 or less, is preferably 5 or less, is more preferably 1 orless, and is further preferably 0.5 or less. When the above additionalmetal components are used in an appropriate combination at adequatecontents, it is possible to achieve high catalytic activity whilemaintaining high selectivity.

In the case where a metal, such as iron or nickel, becomes eluted andenters the catalyst due to the corrosion of a reaction container made ofSS, SUS, or the like, in the first invention, the content of iron andthe contents of the above metals included at specific contents, whichare determined on the basis of the type of material constituting thereaction container, are not taken into account in the calculation of thecontent of the metal components in the catalyst.

In order to further increase the activity of the catalyst, reactionselectivity, and the like, the first catalyst may include compounds ofone or more alkali metal elements selected from the group consisting oflithium, sodium, potassium, rubidium, and cesium; compounds of one ormore alkaline-earth metal elements selected from the group consisting ofmagnesium, calcium, strontium, and barium; and compounds of one or morehalogen elements selected from the group consisting of fluorine,chlorine, bromine, and iodine, in addition to the metal componentsdescribed above. In such a case, the ratio between the additionalcomponents and the rhenium component is nor. limited.

<Carrier>

The carrier used in the first invention is a carrier that includes anoxide of a metal belonging to Group 4 of the periodic table. Inparticular, an inert carrier can be used. The term “inert carrier” usedherein refers to a carrier that does not have a catalytic activity in ahydrogenation or a carbonyl compound alone. Specifically, the inertcarrier is defined as a carrier that substantially does not include anyof the metals belonging to Group 8 to 12 of the periodic table which isselected from the group consisting oi iron, ruthenium, cobalt, rhodium,iridium, nickel, palladium, platinum, copper, and zinc, chromium, andrhenium, which are metals having catalytic activity.

A carrier that substantially does not include any cf the above metals isa carrier that does not primarily include any of the above metals. Thatis, the amount of the above metals included in the carrier to the totalmass of the carrier is 5% by mass or less, is preferably 1% by mass orless, and is mere preferably 0.1% by mass or less. The content of theabove metals in the carrier can be determined as in the analysis of thecontent of the supported metal in the catalyst, using publicly knownanalysis methods, such as inductively coupled plasma mass spectrometry(ICP-MS), inductively coupled plasma atomic emission spectrometry(ICP-AES), atomic absorption spectrometry (AAS), and X-ray fluorescenceanalysis (XRF).

In the first invention, a carrier that includes an oxide of a metalbelonging to Group 4 of the periodic table, such as titanium oxide(titania), zirconium oxide (zirconia), or hafnium oxide, is used inorder to increase catalytic activity and reaction selectivity achievedparticularly when a carboxylic acid is used as a raw material and easeof regeneration of the catalyst and reduce the elution of metals. Amongthe oxides of metals belonging to Group 4 of the periodic table,titanium oxide and zirconium oxide are preferable in order to increasecatalytic activity and produce an intended alcohol with highselectivity. Among these, titanium oxide may be particularly preferablein order to readily produce carrier particles having a large specificsurface area. The oxides of metals belonging to Group 4 of the periodictable may be used alone or in combination of two or more. In the casewhere the oxides of metals belonging to Group 4 of the periodic tableare used in combination of two or more, the combination of the oxidesarid the mixing ratio between the oxides are not limited. The oxides canbe used in a form similar to a mixture of the individual compounds or acomposite oxide.

It may be preferable that the carrier used in the first inventioncontain a sulfate ion. In particular, in the case where titanium oxideis used as a carrier, it may fee preferable that the carrier contain asulfate ion.

In the first invention, using a carrier including a sulfate ion maymarkedly reduce a degradation reaction involved by decarboxylation and adefunctionalization reaction associated with dehydration andhydrogenation of the reaction product, that is, an alcohol, which occursimultaneously with a catalytic reaction of hydrogenation of a carbonylcompound. In addition, when the metal components that include rheniumand the second components are supported on such a carrier, the catalyticactivity of the hydrogenation catalyst may be markedly increased. Whenthe metal components are used in combination with the carrier, thecatalyst can be handled in the air atmosphere. This increases ease ofoperation of the catalyst, such as transportation and storage of thecatalyst and introduction of the catalyst to a reactor in the productionof an alcohol.

It is considered that the functions of the catalyst are enhanced for thefollowing reasons: when the carrier contains a sulfate ion, sulfate ionspresent in the surface of the carrier may form acid sites on the surfaceof the catalyst. Furthermore, the dispersibility of the supported metalmay be increased due to the interaction between the supported metal andthe sulfate ion or a substitution reaction of the supported metal withthe sulfate ion which occurs when the metal components are supported onthe carrier. Moreover, the electronic state of rhenium, which is acatalytic activity component of the hydrogenation catalyst, can becontrolled to be in a state suitable for a reduction reaction of acarbonyl functional group. The above factors may synergisticallyincrease the reaction selectivity of the catalyst and the activity ofthe catalyst.

The mass ratio of the amount of the sulfate ion included in the carrierto the total mass of the carrier used is preferably 0.01% by mass ormore, is more preferably 0.1% by mass or more, and is particularlypreferably 0.2% by mass or more. The mass ratio of the amount of thesulfate ion to the total mass of the carrier used is preferably 10% bymass or less, Is more preferably 7% by mass or less, and is particularlypreferably 5% by mass or less.

When the content of the sulfate ion in the carrier used is limited to beequal to or more than the lower limit, the advantageous effects ofadding the above components are achieved at a sufficient level and highcatalytic activity can be achieved, furthermore, the occurrence of thedefunctionalization reaction can be further reduced. This limits anincrease in the complexity of the process for purifying the reactionproduct and an increase in the purification costs and consequentlyenables an economically advantageous alcohol production process to beprovided. Limiting the content of the sulfate ion in the carrier used tohe equal to or less than the upper limit reduces, for example, corrosionof the reactor caused by sulfate ions included in the carrier becomingeluted during the reaction depending on the solvent used and sidereactions of the target product caused by the liberated acid catalystand therefore eliminates the need to use materials having high corrosionresistance. This limits increases in the costs for constructing reactionfacilities and the costs for purifying the product and enables aneconomically advantageous alcohol production process to be provided.

In the case where a carrier including a sulfate ion is used in the firstinvention, the carrier is not limited and may be any carrier thatincludes a sulfate ion. An appropriate commercial product may be useddirectly. In the case where the carrier is composed of a metal oxide,the carrier may be prepared by, for example, dissolving a correspondingmetal sulfate in water and subsequently performing neutralization orpyrohydrolysis, or by treating a corresponding metal hydroxide or abaked metal oxide with a sulfatizing agent and subsequently performingbaking in an oxidizing atmosphere, such as the air atmosphere. Thetreatment using a sulfatizing agent is to introduce sulfate ions intothe carrier. This treatment nay be performed in the step of producingthe carrier or nay be performed after the production of the carrier.Examples of the sulfatizing agent include sulfuric acid, persulfuricacid, and the salts thereof. Sulfuric acid, a sulfuric acid salt, and apersulfuric acid salt are preferable. The sulfuric acid salt is notlimited and may be any sulfuric acid salt capable of providing sulfateions when dissolved. Examples of the sulfuric acid salt include ammoniumsulfate, sodium sulfate, and potassium sulfate. The same applies to thepersulfuric acid salt, and examples thereof include ammonium persulfate,sodium persulfate, and potassium persulfate. The above salts may be inthe form of an anhydride or hydrate. Such salts may be preferable insome cases because they are less hazardous than acids and easy tohandle.

A preparation example of the carrier including a sulfate ion accordingto the first invention is described below, taking titanium oxide andzirconium oxide as an example.

Titanium oxide containing a sulfate ion car. be prepared by dissolvingtitanium sulfate or titanyl sulfate in water, subsequently performingneutralization at a low temperature or pyrohydrolysis, and thenperforming baking. Titanium oxide containing a sulfate ion can also beprepared by dissolving titanium ore in sulfuric acid, subsequentlyperforming heating to produce metatitanic acid or titanium hydroxide,and then performing baking.

In another case, titanium oxide containing a sulfate ion may be producedby passing dilute sulfuric acid through titanium hydroxide, which is astarting material, prepared from titanium tetraisopropoxide or the likeand subsequently performing baking in the air atmosphere. Alternatively,a baked titanium oxide may also be used as a starting material insteadof titanium hydroxide. Instead of passing sulfuric acid, a sulfuric acidsalt, such as ammonium 3ulfate, may be supported on the carrier.

The titanium oxide that has been subjected to the sulfatizing treatmentis subsequently baked. The baking temperature is preferably 350° C. to700° C. and is more preferably 450° C. to 600° C. It is not preferableto set the baking temperature to be excessively high because, if thebaking temperature is excessively high, the sulfate ions included in thecatalyst become volatilized and the surface area of the titanium oxidedecreases disadvantageous. The amount of baking time during which thebaking is performed is not limited. It is appropriate to set the bakingtime to about 3 hours.

Examples of a commercial product, of the titanium oxide containing asulfate ion include MC-50, MC-90, and MC-150 produced by Ishihara SangyoKaisha, Ltd., which are also described in Examples of the firstInvention below.

Zirconium oxide containing a sulfate ion can be prepared by, &.& in thepreparation example of the titanium oxide, adding sulfuric acid, asulfate, a persulfate, or the like to a starting material that is, forexample, zirconium hydroxide prepared by adding ammonia wafer to anaqueous solution of a zirconium compound, such as zirconium oxychloride,zirconium oxynitrate, zirconium propoxide, or the like, and subsequentlyperforming baking in the air atmosphere. Alternatively, a bakedzirconium oxide may also be used instead of zirconium hydroxide. Insteadof passing dilute sulfuric acid, a sulfuric acid, such as ammoniumsulfate, may be supported on the carrier.

The zirconium oxide that has been subjected to the sulfatizing treatmentis subsequently baked. The baking temperature is preferably 350° C. to700° C. and is more preferably 450° C. to 600° C. It is not preferableto set the baking temperature to be excessively high because, if thebaking temperature is excessively high, the sulfate ions included in thecatalyst become volatilized and the surface area of the zirconium oxidedecreases disadvantageously. The amount of baking tine during which thebaking is performed is not limited. It is appropriate to set the bakingtime to about 3 hours.

In the case where the carrier is a commercial carrier, the content ofsulfate ion in the carrier has been published by the manufacturer, andthe sulfate ion content falls within the above-described range ofsulfate ion content specified in the first invention, the carrier isconsidered to correspond to the carrier according to the firstinvention. Examples of such a commercial carrier include MC-50, MC-90,and MC-130 produced by Ishihara Sangyo Kaisha, Ltd.

In the case where it is clear that the sulfur element Component of thecarrier is derived from a sulfate ion, alternatively, the content ofsulfate ion in the carrier or catalyst may be determined using apublicly known high-frequency furnace combustion-infrared detectionmethod (carbon sulfur analyzer) by combusting the catalyst in ahigh-frequency induction heating furnace under an oxygen atmosphere andconverting the content of sulfur in the combustion gas into the mass ofsulfate ion, which is determined by an infrared detection method.

In the case where the catalyst according to the first invention containsa sulfate ion, the content of the sulfate ion in the catalyst is notlimited and the mass ratio of the amount of sulfate ion to the totalmass of the catalyst is preferably 0.01% by mass or more, is morepreferably 0.1% by mass or more, is particularly preferably 0.2% by massor wore, is normally 10% by mass or less, is preferably 7% by mass orless, is more preferably 5% by mass or less, is particularly preferably2% by mass or less, and is most preferably 1% by mass or less. The massratio of the amount of sulfur element to the total mass of the catalystis preferably 0.01% by mass or more, is more preferably 0.1% by mass ormore, is normally 3% by mass or less, is preferably 2% by mass or less,is more preferably 1% by mass or less, and is particularly preferably0.6% by mass or less.

Using a catalyst containing a sulfate ion or sulfur may markedly reducea degradation reaction involved by decarboxylation and adefunctionalization reaction associated with dehydration andhydrogenation of the reaction product, that is, an alcohol, which occursimultaneously with a catalytic reaction of hydrogenation of a carbonylcompound. Limiting the content of sulfate ion in the catalyst to beequal to or more than the lower limit, may increase catalytic activityto a sufficient degree and reduce the occurrence of thedefunctionalization reaction to a sufficient degree. This limits anincrease in the complexity of the process for purifying the reactionproduct and an increase in the purification coats and consequentlyenables an economically advantageous alcohol production process to beprovided. Limiting the content of sulfate ion in the catalyst accordingto the present invention to be equal to or more than the lower limitalso enhances the stability of the catalyst in the air atmosphere. Thisincreases ease of operation of the catalyst, such as transportation andstorage of the catalyst and introduction cf the catalyst to a reactor inthe production of an alcohol. Limiting the content of the sulfate ion mthe catalyst to be equal to or less than the upper limit reduces, forexample, corrosion of the reactor caused by sulfate ions included in thecatalyst becoming eluted during the reaction and side reactions of thetarget product caused by the liberated acid catalyst. This limitsincreases in the costs for constructing reaction facilities and thecosts for purifying the target product and enables an economicallyadvantageous alcohol production process to be provided.

In the first invention, the content of the sulfate ion in the carrier orcatalyst is determined by publicly known ion chromatography after thesulfate ion has been extracted from the catalyst in a pretreatment 3tep.

The content of the sulfur in the carrier or catalyst is determined usinga publicly known high-frequency furnace combustion-infrared detectionmethod (carbon sulfur analyzer) by combusting the catalyst in ahigh-frequency induction heating furnace under an oxygen atmosphere andcalculating the content of sulfur in the combustion gas by an infrareddetection method.

The carrier used in the first invention is preferably composed primarilyof the oxide of a metal belonging to Group 4 of the periodic table. Theexpression “composed primarily of” used herein means that the mass ratioof the oxide of a metal belonging to Group 4 of the periodic table tothe total mass of the carrier is normally 50% by mass or more, ispreferably 70% by mass or more, and is more preferably 90% to 100% bymass.

The carrier used in the first invention may include a carrier componentother than the oxide of a metal belonging to Group 4 of the periodictable. Examples of the other carrier component include one or morecompounds selected from graphite, active carbon, silicon carbide,silicon nitride, aluminum nitride, boron nitride, boron oxide, aluminumoxide (alumina), silicon oxide (silica), lanthanum oxide, cerium oxide,yttrium oxide, niobium oxide, magnesium silicate, calcium silicate,magnesium aiuminate, calcium aluminate, aluminosilicate,aluminosilicophosphate, aluminophosphate, magnesium phosphate, calciumphosphate, strontium phosphate, apatite hydroxide (calciumhydroxyphosphate), apatite chloride, apatite fluoride, calcium sulfate,barium sulfate, and barium carbonate.

The specific surface area of the carrier particles used in the firstinvention varies by the type of the carrier used and is not limited. Thespecific surface area of the carrier particles used in the firstinvention is normally 50 m²/g or more, is preferably 80 m²/g or more, ismore preferably 100 m²/g or more, is normally 3000 m²/g or less, and ispreferably 2000 m²/g or less. In particular, in the first invention inwhich the oxide of a metal belonging to Group 4 of the periodic table isused, the specific surface area of the carrier particles is normally 50m²/g or more, is preferably 80 m²/g or more, is more preferably 100 m²/gor more, is normally 1000 m²/g or less, and is preferably 800 m²/g orless. The larger the specific surface area of the carrier particles, thehigher the catalytic activity. Therefore, carrier particles having alarger specific surface area are suitably used. The specific surfacearea of the carrier particles is generally calculated from the amount ofnitrogen adsorbed on the carrier particles using the BET equation.

The shape and size of the carrier particles used in the first inventionare not limited. When the shape of the carrier particles is convertedinto a spherical shape, the average particle size of the carrier isnormally 0.1 μm or more, is preferably 3 μm or more, is more preferably5 μm or more, is further preferably 50 μm or more, is normally 5 mm orless, and is preferably 4 mm or less. The particle size of the carrieris measured in accordance with Test sieving described in JIS StandardJIS Z8815 (1894). In the case where the shape of a carrier particle isnot spherical, the volume of the carrier particle is measured, thediameter of a spherical particle having the same volume as the carrierparticle is calculated, and the diameter of the spherical particle isconsidered the diameter of the carrier particle. When the averageparticle size of the carrier falls within the above range, the activityof the catalyst per unit mass is increased, and ease of handling of thecatalyst is further increased.

In the case where the reaction conducted using the first catalyst is acomplete mixing reaction, the average particle size of the carrier isnormally 0.1 μm or more, is preferably 1 μm or more, is more preferably5 μm or more, is further preferably 50 μm or more, is normally i ism orless, and is preferably 2 mm or less. It is preferable to reduce theaverage particle size of the carrier because the smaller the averageparticle size of the carrier, the higher the activity of the catalystper unit mass. However, setting the average particle size of the carrierto be excessively smaller than the above lower limit may make itdifficult to separate the reaction liquid and the catalyst from eachother.

In the case where the reaction conducted using the first catalyst is afixed-bed reaction, the average particle size of the carrier is normally0.5 mm or snore and 5 mm or less, is preferably 4 mm or less, and ismore preferably 3 mm or less. If the particle size of the carrier isexcessively smaller than the above lower limit, it may become difficultto operate a reaction facility due to pressure difference. If theparticle size of the carrier is excessively larger than the above upperlimit, reaction activity may be reduced.

Catalyst According to Second Invention

A catalyst according to the second invention (hereinafter, may bereferred to simply as “second catalyst”) is a metal-supporting catalystthat includes a metal component and a carrier on which the metalcomponent is supported. Specifically, the metal components including afirst component that is rhenium and one or more second componentsselected from the group consisting of silicon, gallium, germanium, andindium are supported on a carrier. The mass ratio of the amount of thesecond components to the amount of rhenium is set to a predeterminedvalue.

The second catalyst is normally produced by reducing a metal-supportingmaterial on which the metal component is supported with a reducing gasand then performing an oxidative stabilization treatment as needed.

<Metal Component>

The metal component supported on the metal-supporting catalyst accordingto the second invention includes a first component that is rhenium andone or more second components selected from the group consisting ofsilicon, gallium, germanium, and indium. Among these, the secondcomponents used in combination with rhenium are preferably one or moreelements selected from the group consisting of silicon, germanium, andindium, are more preferably one or more elements that include indiumand/or germanium, are further preferably one or more elements thatinclude germanium, and are particularly preferably germanium.

As for the ratio between the amounts of the above essential componentssupported on the catalyst, the lower limit for the mass ratio of thesecond component elements that are one or more elements selected fromthe group consisting of silicon, gallium, germanium, and indium to therhenium element is preferably 0.1 or more and is more preferably 0.5 ormore, and the upper limit for the above mass ratio is preferably 30 orless, is more preferably 5 or less, is further preferably 3 or less, isparticularly preferably 2 or less, and is most preferably 3 or less.

Appropriately selecting the types of the second components used incombination with rhenium and/or the proportion of the second componentssupported on the carrier increases the catalytic activity in ahydrogenation reaction of a carbonyl compound and makes it possible toproduce an alcohol while reducing side reactions, such as anesterification reaction of a carboxylic acid used as a raw material withan alcohol produced, and a defunctionalization reaction due to thedehydration and hydrogenation of the alcohol produced, whichsignificantly occurs particularly at a later stage of the reaction, to ahigh degree. Using the above metal components in combination with oneanother enables the second catalyst to be handled in the air atmosphere.This increases ease of operation, such as transportation and storage ofthe catalyst and introduction of the catalyst to a reactor in theproduction of an alcohol.

Using the above metal components in combination with each other enablesan increase in catalytic activity and an increase in reactionselectivity, which have been considered contradictory, to be bothachieved presumably for the following reasons: the addition of thesecond components enables the electronic state of rhenium, which is acatalytic activity component of the hydrogenation catalyst, to becontrolled to be in a state suitable for a reduction reaction of acarbonyl functional group; the adsorptivity of reactive substrates ontothe surface of the catalyst is enhanced due to the affinity of thereactive substrates for the second components; and the orientation ofadsorption of the reactive substrates on the surface of the catalyst iscontrolled at a high degree.

Although the amount of rhenium, supported on the second catalyst is notlimited, the mass ratio of the rhenium element to the total mass of themetal-supporting catalyst is normally 0.5% by mass or more, ispreferably 1% by mass or more, is more preferably 3% by mass or more, isnormally 20% by mass or less, is preferably 10% by mass or. less, and ismore preferably 8% by mass or less. When the amount of rhenium supportedon the catalyst is limited to be equal to or more than the lower limit,sufficiently high catalytic activity can be achieved. This prevents, forexample, an increase in the sire of the reactor used. When the amount ofrhenium supported on the catalyst is limited to be equal to or less thanthe upper limit, an increase in the cost of the catalyst can be limited.Furthermore, in such a case, coagulation of rhenium supported on thecatalyst can be reduced. This reduces the side reactions, such as adegradation reaction involved fey decarboxylation, a defunctionalizationreaction associated with dehydration and hydrogenation of. the reactionproduct, and an esterification reaction of a carboxylic acid used as araw material with an alcohol produced, due to high Lewis acidity ofrhenium. As a result, reaction selectivity can be further increased.

The second catalyst may further include, as needed, a third componentthat is a metal component other than the above metal components (i.e.,rhenium and the second components) and that does not adversely affectthe reactions conducted using the second catalyst, such as a reductionreaction. Examples of the Other metal component include metal componentsbelonging to Groups 8 to 10 of the periodic table except iron andnickel. Examples thereof include at least one metal selected from thegroup consisting of ruthenium, cobalt, rhodium, iridium, palladium, andplatinum, which are capable of catalyzing hydrogenation. Note that theterm “periodic table” used herein refers to the long form of periodictable (.Nomenclature of Inorganic Chemistry IUPAC Recommendations 2005).

Metals, such as iron and nickel, may elute and enter the catalyst when ametal reaction container made of SS, SUS, or the like becomes corrodedin the preparation of the catalyst and/or the reaction. In the secondinvention, in the case where the eluted metal is precipitated on thecatalyst and included in the catalyst, the metal is not defined as ametal component of the second catalyst. In the case of elution from areaction container made of SUS, in addition to iron, the followingmetals may be detected in the catalyst in trace amounts at specificcontents depending on the material used.

For example, when metals enter from SUS201, nickel, chromium, andmanganese may be detected in addition to iron at specific contents. Whenmetals enter from SUS202, nickel chromium, and manganese may teedetected in addition to iron at specific contents. When metals enterfrom SUS301, nickel and chromium may be detected in addition to iron atspecific contents. When metals enter from SUS302, nickel and chromiummay be detected in addition to iron at specific contents. When metalsenter from SUS202, nickel, chromium, and molybdenum may be detected inaddition to iron at specific contents. When metals enter from SUS304,nickel and chromium may be detected in addition to iron at. specificcontents. When metals enter from SUS305, nickel and chromium may bedetected in addition to iron at specific contents. When metals enterfrom SUS316, nickel, chromium, and molybdenum may be detected inaddition to iron at specific contents. When metals enter from SUS317,nickel, chromium, and molybdenum may be detected in addition to iron atspecific contents. When metals enter from SUS329J1, nickel, chromium,and molybdenum may be detected in addition to iron at specific contents.When metals enter from SUS403, chromium may be detected in addition toiron at a specific content. When metals enter from SUS405, chromium andaluminum may be detected in addition to iron at specific contents. Whenmetals enter from SUS420, chromium may be detected in addition to ironat a specific content. When metals enter from SUS430, chromium may bedetected in addition to iron at a specific content. When metals enterfrom SUS430LX, chromium, titanium, or niobium may be detected inaddition to iron at a specific content. When metals enter from SUS630,nickel, chromium, copper, and niobium may be detected in addition toiron at specific contents.

Examples of the metal component that belongs to a group other thanGroups 8 to 10 of the periodic table include at least one metal selectedfrom the group consisting of silver, gold, molybdenum, tungsten,aluminum, and boron.

Among the above third components, at least one metal selected fromruthenium, cobalt, rhodium, iridium, palladium, platinum, gold,molybdenum, and tungsten is preferable; at least one metal selected fromruthenium, cobalt, rhodium, iridium, palladium, platinum, molybdenum,and tungsten is more preferable; at least one metal selected fromruthenium, iridium, palladium, and platinum is particularly preferable;and ruthenium is most preferable.

In the case where the third component is selected from rare andexpensive metals belonging to Groups 8 to 10 of the periodic tableexcept iron and nickel, the elemental mass ratio of the third componentincluded in the second catalyst to the rhenium element is normally lessthan 0.2, is preferably 0.15 or less, is more preferably 0.1 or less, isfurther preferably less than 0.1, and is most preferably 0 in order toincrease reaction selectivity and economical efficiency in terns of thecosts for producing the catalyst. That is, it is preferable that thesecond catalyst substantially do not include any of the rare andexpensive metals belonging to Groups 8 to 10 of the periodic table etherthan iron or nickel.

In the case where the third component is selected from metals other thanthe noble metals belonging to Groups 8 to 10 of the periodic table, theelemental mass ratio of the third component to the rhenium element isnormally 10 or less, is preferably 5 or less, is more preferably 1 orless, and is further preferably 0.5 or less. When the above additionalmetal components are used in an appropriate combination at adequatecontents, it rs possible to achieve high catalytic activity whilemaintaining high selectivity.

In the case where a metal, such as iron or nickel, becomes eluted andenters the catalyst due to the corrosion of a reaction container made ofSS, SUS, or the like, in the second invention, the content of iron andthe contents of the above metals included at specific contents, whichare determined on the basis of the type of material constituting thereaction container, are not taken into account in the calculation of thecontent of the metal components in the catalyst.

In order to further increase the activity of the catalyst, reactionselectivity, and the like, the second catalyst may include compounds ofone or more alkali metal elements selected from the group consisting oflithium, sodium, potassium, rubidium, and cesium; compounds of one ormore alkaline-earth metal elements selected from the group consisting ofmagnesium, calcium, strontium, and barium; and compounds of one or merehalogen elements selected from the group consisting of fluorine,chlorine, bromine, and iodine, in addition to the metal componentsdescribed above. In such a case, the ratio between the additionalcomponents and the rhenium component is not limited.

<Carriar>

The carrier used in the second invention is not limited. In particular,an inert carrier can be used. The term “inert carrier” used hereinrefers to a carrier that does not have a catalytic activity in ahydrogenation of a carbonyl compound alone. Specifically, the inert,carrier is defined as a carrier that substantially does not include anyof the metals belonging to Group 8 to 12 of the periodic table which isselected from the group consisting of iron, ruthenium, cobalt, rhodium,iridium, nickel, palladium, platinum, copper, and zinc, chromium, andrhenium, which are metals having catalytic activity.

In the second invention, a carrier that substantially does not includeany of the -above metals is a carrier that does not primarily includeany of the above metals. That is, the amount of the above metalsincluded in the carrier to the total mass of the carrier is 5% by massor less, is preferably 1% by mass or less, and is more preferably 0.1%by mass or less. The content of the above metals in the carrier can bedetermined as in the analysis of the content of the supported metal inthe catalyst, using publicly known analysis methods, such as inductivelycoupled plasma mass spectrometry (ICP-MS), inductively coupled plasmaatomic emission spectrometry (ICP-AES), atomic absorption spectrometry(AAS), and X-ray fluorescence analysis (XRF).

Examples of the inert carrier used in the second invention includes acarrier composed primarily of an element other than the metals belongingto Groups 8 to 12 of the periodic cable, such as iron, ruthenium,cobalt, rhodium, iridium, nickel, palladium, platinum, copper, and zinc,chromium, or rhenium; a carrier composed primarily of a carbide, anitride, an oxide, a hydroxide, a sulfuric acid salt, a carbonic acidsalt, or a phosphoric acid salt of the element; and a carrier composedprimarily of a mixture of the above substances. The expression “composedprimarily of” used herein means that the mass ratio of the substance tothe total mass of the carrier is normally 50% by mass or more, ispreferably 70% by mass or more, and is more preferably 90% by mass ormore.

Specific examples of the carrier according to the second inventioninclude graphite, active carbon, silicon carbide, silicon nitride,aluminum nitride, boron nitride, boron oxide, aluminum oxide (alumina),silicon oxide (silica), titanium oxide (titania), zirconium oxide(zirconia), hafnium oxide, lanthanum oxide, cerium oxide, yttrium oxide,niobium oxide, magnesium silicate, calcium silicate, magnesiumaluminate, calcium aluminate, aluminosilicate, aluminosilicophosphate,aluminophosphate, magnesium phosphate, calcium phosphate, strontiumphosphate, apatite hydroxide (calcium hydroxyphosphate), apatitechloride, apatite fluoride, calcium sulfate, barium sulfate, and bariumcarbonate.

Among these, a carbonaceous carrier, titanium oxide, zirconium oxide,niobium oxide, and cerium oxide are preferable in order to increasecatalytic, activity and reaction selectivity achieved particularly whena carboxylic acid is used as a raw material and reduce the elution ofmetals. Among the above substances, titanium oxide, zirconium oxide,niobium oxide, and cerium oxide are preferable in order to increase caseof the regeneration treatment of the catalyst. Among the abovesubstances, titanium oxide and zirconium oxide, which are oxides ofmetals belonging to Group 4 of the periodic table, are more preferable.Titanium oxide may be particularly preferable in order to readilyproduce carrier particles having a large specific surface area.

The above carriers may be used alone or in combination of two or more.In the case where the carriers are used in combination of two or more,the combination of the carriers and the mixing ratio between thecarriers are not limited. The carriers can be used in a form similar toa mixture of the individual compounds, a composite compound, or a doublesalt.

The carrier may be used directly or may be subjected to a pretreatmentin which the carrier particles are formed into a shape suitable forsupporting the metal components thereon. For example, in the case wherea carbonaceous carrier is used, the carbonaceous carrier may besubjected to a heating treatment using nitric acid before use, asdescribed in Japanese Unexamined Patent Application Publication No.10-71332. It is preferable to use the above method in order to enhancethe dispersibility of the metal components on the carrier and therebyincrease the activity of the catalyst.

It may be preferable that the carrier used in the second inventioncontain a sulfate ion. In particular, in the case where titanium oxideis used as a carrier, it may be preferable that the carrier contain asulfate ion.

In the second invention, using a carrier including a sulfate ion maymarkedly reduce a degradation reaction involved by decarboxylation and adefunctionalization reaction associated with dehydration andhydrogenation of the reaction product, that is, an alcohol, which occursimultaneously with a catalytic reaction of hydrogenation of a carbonylcompound. In addition, when the metal components that include rheniumand the second components are supported on such a carrier, the catalyticactivity of the hydrogenation catalyst may be markedly increased. Whenthe metal components are used in combination with the carrier, thecatalyst can be handled in the air atmosphere. This increases ease ofoperation of the catalyst, such as transportation and storage of thecatalyst and introduction of the catalyst to a reactor in the productionof an alcohol.

It is considered that the functions of the catalyst are enhanced for thefollowing reasons: when the carrier contains a sulfate ion, sulfate ionspresent in the surface of the carrier may form acid 3ites on the surfaceof the catalyst. Furthermore, the dispersibility of the supported metalmay be increased due to the interaction between the supported metal andthe sulfate ion or a substitution reaction of the supported metal withthe sulfate ion which occurs when the metal components are supported onthe carrier. Moreover, the electronic state of rhenium, which is acatalytic activity component oI the hydrogenation catalyst, can becontrolled to be in a state suitable for a reduction reaction of acarbonyl functional group. The above factors may synergisticallyincrease the reaction selectivity of the catalyst and the activity ofthe catalyst.

The mass ratio of the amount of the sulfate ion included in the carrierto the total mass of the carrier used is preferably 0.01% by mass ormore, is more preferably 0.1% by mass or more, and is particularlypreferably 0.2% by mass or more. The mass ratio of the amount of thesulfate ion to the total mass of the carrier used is preferably 10% bymass or less, is more preferably 7% by mass or less, and is particularlypreferably 5% by mass or less.

When the content of the sulfate ion in the carrier used is limited to beequal to or more than the lower limit, the advantageous effects ofadding the above components are achieved at. a sufficient level and highcatalytic activity can be achieved. Furthermore, the occurrence of thedefunctionalization reaction can be further reduced. This limits anincrease in the complexity of the process for purifying the reactionproduct and an increase in the purification costs and consequentlyenables an economically advantageous alcohol production process to beprovided. Limiting the content of the sulfate ion in the carrier used tobe equal to or less than the upper limit reduces, for example, corrosionof the reactor caused by sulfate ions included in the carrier becomingeluted during the reaction depending on the solvent used and sidereactions of the target product caused by the liberated acid catalystand therefore eliminates the need to use materials having high corrosionresistance. This limits increases in the costs for constructing reactionfacilities and the costs for purifying the product and enables aneconomically advantageous alcohol production process to be provided.

In the case where a carrier, including a sulfate ion is used in the3eccnd invention, the carrier is not limited and may be any carrier thatincludes a sulfate ion. An appropriate commercial product may be useddirectly. In the case where the carrier is composed of a metal oxide,the carrier may be prepared by, for example, dissolving a correspondingmetal sulfate in water and subsequently performing neutralization orpyrohydrolysis, or by treating a corresponding metal hydroxide or abaked metal oxide with a sulfatizing agent and subsequently performingbaking in an oxidizing atmosphere, such as the air atmosphere. Thetreatment using a sulfatizing agent is to introduce sulfate ions intothe carrier. This treatment may foe performed in the step of producingthe carrier or may be performed after the production of the carrier.Examples of the sulfatizing agent include sulfuric acid, persulfuricacid, and the salts thereof. Sulfuric acid, a sulfuric acid salt, and apersulfuric acid salt are preferable. The sulfuric acid salt is notlimited and may be any sulfuric acid salt capable of providing sulfateions when dissolved. Examples cf the sulfuric acid salt include ammoniumsulfate, sodium sulfate, and potassium sulfate. The same applies to thepersulfuric acid salt, and examples thereof include ammonium persulfate,sodium persulfate, and potassium persulfate. The above salts may be inthe form of an anhydride or hydrate. Such salts may be preferable insome cases because they are Ie3s hazardous than ac.id3 and easy tohandle.

A preparation example of the carrier including a sulfate ion accordingto the second invention is described below, taking titanium oxide andzirconium oxide as an example.

Titanium oxide containing a sulfate ion can be prepared by dissolvingtitanium sulfate or titanyl sulfate in water, subsequently performingneutralization at a low temperature or pyrohydrolysis, and thenperforming baking. Titanium oxide containing a sulfate ion can also beprepared by dissolving titanium ore in sulfuric acid, subsequentlyperforming heating to produce metatitanic acid or titanium hydroxide,and then performing baking.

In another case, titanium oxide containing a sulfate ion may be producedby passing dilute sulfuric acid through titanium hydroxide, which is astarting material, prepared from titanium tetraisopropoxide or the likeand subsequently performing baking in the air atmosphere. Alternatively,a baked titanium oxide may also be used as a starting material insteadof titanium hydroxide. Instead of passing sulfuric acid, a sulfuric acidsalt, such as ammonium sulfate, may be supported on the carrier.

The titanium oxide that has been subjected to the sulfatizing treatmentis subsequently baked. The baking temperature is preferably 350° C. to700° C. and is mere preferably 450° C. to 600° C. It is not preferableto set the baking temperature to be excessively high because, if thebaking temperature is excessively high, the sulfate ions included in thecatalyst become volatilized and the surface area of the titanium oxidedecreases disadvantageously. The amount of baking time during which thebaking is performed is not limited. It is appropriate to set the bakingtime to about 3 hours.

Examples of a commercial product of the titanium oxide containing asulfate ion include MC-30, MC-90, and MC-150 produced by Ishihara SangyoKaisha, Ltd., which are also described in Examples of the secondinvention below.

Zirconium oxide containing a sulfate ion can be prepared by, as in thepreparation example of the titanium oxide, adding sulfuric acid, asulfate, a persulfate, or the like to a starting material that is, forexample, zirconium hydroxide prepared by adding ammonia water to anaqueous solution of a zirconium compound, such as zirconium oxychloride,zirconium oxynitrate, zirconium propoxide, or the like, and subsequentlyperforming baking in the air atmosphere. Alternatively, a bakedzirconium oxide may also be used instead of zirconium hydroxide. Insteadof passing dilute sulfuric acid, a sulfuric acid, such as ammoniumsulfate, may be supported on the carrier.

The zirconium oxide that has been subjected to the sulfatizing treatmentis subsequently baked. The baking temperature is preferably 350° C. to700° C. and is more preferably 450° C. to 600° C. It is not preferableto set the baking temperature to be excessively high because, it thebaking temperature is excessively high, the sulfate ions included in thecatalyst become volatilized and the surface area of. the zirconium oxidedecreases disadvantageously. The amount of baking time during which thebaking is performed is not limited. It is appropriate to set the bakingtime to about 3 hours.

In the case where the carrier is a commercial carrier, the content ofsulfate ion in the carrier has been published by the manufacturer, andthe sulfate ion content falls within the above-described range ofsulfate ion content specified in the second invention, the carrier isconsidered to correspond to the carrier according to the secondinvention. Examples of such a commercial carrier include MC-50, MC-90,and MC-150 produced by Ishihara Sangyo Kaisha, Ltd.

In the case where it is clear that the sulfur element component of thecarrier is derived from a sulfate ion, alternatively, the content ofsulfate ion in the carrier or catalyst may be determined using apublicly known high-frequency furnace combustion-infrared detectionmethod (carbon sulfur analyzer) by combusting the catalyst in ahigh-frequency induction heating furnace under an oxygen atmosphere andconverting the content of sulfur in the combustion gas into the mass ofsulfate ion, which is determined by an infrared detection method.

In the case where the catalyst according to the second inventioncontains a sulfate ion, the content of the sulfate ion ,i.n the catalystis not limited and the mass ratio of the amount of. sulfate ion to thetotal mass of the catalyst is preferably 0.01% by mass or more, is morepreferably 0.1% by mass or more, is particularly preferably 0.2% by massor more, is normally 10% by mass or less, is preferably 1% by mass orleas, is more preferably 5% by mass or less, is particularly preferably2% by mass or less, and is most preferably 1% by mass or less. The massratio of the amount of sulfur element to the total mass of the catalystis preferably 0.01% fey mass or more, is more preferably 0.1% by mass ormore, is normally 3% by mass or less, is preferably 2% by mass or less,is more preferably 1% by mass or less, and is particularly preferably0.6% by mass or less.

Using a catalyst containing a sulfate ion or sulfur may markedly reducea degradation reaction involved by decarboxylation and adefunctionalization reaction associated with dehydration andhydrogenation of the reaction product, that is, an alcohol, which occursimultaneously with a catalytic reaction of hydrogenation of a carbonylcompound. Limiting the content of sulfate ion in the catalyst to beequal to or more than the lower limit may increase catalytic activity toa sufficient degree and reduce the occurrence of the defunctionalizationreaction to a sufficient degree. This limits an increase in thecomplexity of the process for purifying the reaction product and anincrease in the purification costs and consequently enables aneconomically advantageous alcohol production process to be provided.Limiting the content of sulfate ion in the catalyst according to thepresent invention to be equal to or more than the lower limit alsoenhance, the stability of the catalyst in the air atmosphere. Thisincreases ease of operation of the catalyst, such as transportation andstorage of the catalyst and introduction of the catalyst to a reactor inthe production of an alcohol. Limiting the content of the sulfate ion inthe catalyst to be equal to or less than the upper limit reduces, forexample, corrosion of the reactor caused by sulfate ions included in thecatalyst becoming eluted during the reaction and side reactions of thetarget product caused by the liberated acid catalyst. This limitsincreases in the costs tor constructing reaction facilities and thecosts for purifying the target product and enables an economicallyadvantageous alcohol production process to be provided.

In the second invention, the content of the sulfate ion in the carrieror catalyst is determined by publicly known ion chromatography after thesulfate ion has been extracted from the catalyst in a pretreatment step.

The content of the sulfur in the carrier or catalyst is determined usinga publicly known high-frequency furnace combustion-infrared detectionmethod (carbon sulfur analyzer) by combusting the catalyst in ahigh-frequency induction heating furnace under an oxygen atmosphere andcalculating the content of sulfur in the combustion gas by an infrareddetection method.

The specific surface area of the carrier particles used in the secondinvention varies by the type of the carrier used and is not limited. Thespecific surface area of the carrier particles used in the secondinvention is normally 50 m²/g or more, is preferably 80 m²/g or more, ismore preferably 100 m²/g or more, is normally 3000 m²/g or loss, and ispreferably 2000 m²/g or leas. In the case where a metal oxide is used asa carrier, the specific surface area of the carrier particles isnormally 50 m²/g or more, is preferably 80 m²/g or more, is morepreferably 100 m²/g or more, is normally 1000 m²/g or less, and ispreferably 800 m²/g or less. The larger the specific surface area of thecarrier particles, the higher the catalytic activity. Therefore, carrierparticles having a larger specific surface area are suitably used. The.specific surface area of the carrier particles is generally calculatedfrom the amount of nitrogen adsorbed on the carrier particles using theBET equation.

The shape and size of the carrier particles used in the second inventionare not limited. When the shape of the carrier particles is convertedinto a spherical shape, the average particle size of the carrier isnormally 0.1 μm or more, is preferably 1 μm or more, is more preferably5 μm or more, is further preferably 50 μm or mere, is normally 5 mm orless, and is preferably 4 mm or less. The particle size of the carrieris measured in accordance with Test sieving described in JIS StandardJIB Z8815 (1994). In the case where the shape of a carrier particle isnot spherical, the volume of the carrier particle is measured, thediameter of a spherical particle having the same volume as the carrierparticle is calculated, and the diameter of the spherical particle isconsidered the diameter of the carrier particle. When the averageparticle size of the carrier falls within the above range, the activityof the catalyst per unit mass is increased, and ease of handling of thecatalyst rs further increased.

In the case where the reaction conducted using the second catalyst is acomplete mixing reaction, the average particle size of the carrier isnormally 0.1 μm or more, is preferably 1 μm or more, is more preferably5 μm or more, is further preferably 50 μm or more, is normally 3 μm orless, and is preferably 2 nun or less. It is preferable to reduce theaverage particle size of the carrier because the smaller the averageparticle size of the carrier, the higher the activity of the catalystper unit mass. However, setting the average particle size of. thecarrier to be excessively smaller than the above lower limit may make itdifficult to separate the reaction liquid and the catalyst from eachother.

In the case where the reaction conducted using the second main catalystis a fixed-bed reaction, the average particle size of the carrier isnormally 0.5 mm or mere and 5 mm or less, is preferably 4 mm or less,and is more preferably 3 mm or less. If the particle size of the carrieris excessively smaller than the above lower limit, it may becomedifficult to operate a reaction facility due to pressure difference. Ifthe particle size of the carrier is excessively larger than the aboveupper limit, reaction activity may be reduced.

[Method for Producing This Catalyst]

The method for producing the first catalyst and the second catalyst(hereinafter, they are referred to as “this catalyst”) normally includesthe following steps.

(i) a step in which, the metal components are attached to the carrier(hereinafter, this step is referred to as “metal attachment step”))

(ii) a step in which the resulting metal-supporting material issubjected to a reduction treatment using a reducing gas (hereinafter,this step is referred to as “reduction treatment step”))

(iii) a step in which oxidation is performed as needed subsequent to thereduction treatment, (hereinafter, this step is referred to as“oxidative stabilization step”))

Each of the above steps is described below.

<(i) Metal Attachment Step>

The metal attachment step is a step in which required amounts of theabove-described metal components are attached to the above-describedcarrier in order to prepare a metal-supporting material. The method forattaching the metal components to the carrier is not limited, andpublicly known methods can be used. For attaching the metal componentsto the carrier, a solution or dispersion liquid containingmetal-containing compounds that are raw materials tor the metalcomponents can be used.

The method for attaching the metal components to the carrier is notlimited. Normally, various impregnation methods may be used. Examplesthereof include an adsorption method in which metal ions are caused toadsorb to the carrier in an amount equal to or less than the salutationamount of the metal ions adsorbed by using the ability of the metal ionsto adsorb to the carrier; an equilibrium adsorption method in which thecarrier is immersed in the solution containing an amount of metal ionswhich is equal to or more than the saturation amount of the metal ionsadsorbed and the excess solution is removed; a pore-filling method inwhich the solution having the same, volume as the pores formed in thecarrier is added to the carrier and the whole amount of the solution iscaused to adsorb to the carrier; an incipient wetness method in whichthe solution is added t.o the carrier until the volume of the solutionadded is appropriate to the water absorption capacity of the carrier andthe treatment is terminated when the surfaces of the carrier particlesbecome uniformly wet and excess solution is not present on the surfacesof the carrier particles; an evaporation-to-dryness method in which thecarrier is impregnated with the solution and the solvent is removed byevaporation while the solution is stirred; and a spray method in whichthe carrier is dried and the solution is sprayed to the dried carrier.Among these, the pore-filling method, the incipient wetness method, theevaporation-to-dryness method, and the spray method are preferable, andthe pore-filling method, the incipient wetness method, and theevaporation-to-dryness method are more preferable. Using the abovepreparation methods enables rhenium, the above-described secondcomponent, and the optional third component and the other metalcomponents which may be added to the catalyst as needed to be supportedon the carrier while being relatively uniformly dispersed on thecarrier. As described in the first and second inventions above, it maybe preferable that the carrier include a sulfate ion. In such a case, itis preferable to attach the metal components to a carrier that includesan amount of sulfate ion which is 0.01% by mass or more and 10% by massor less of the mass of the carrier.

The metal-containing compounds used are not limited and may be selectedappropriately in accordance with the attaching method used. Examplesthereof include halides, such as a chloride, a bromide, and an iodide;mineral acid salts, such as a nitric acid salt and a sulfuric acid salt;metal hydroxides; metal oxides; metal-containing ammonium salts;organic-group-containing compounds, such as an acetic acid salt and ametal alkoxide; and metal complexes. Among these, halides, mineral acidsalts, metal hydroxides, metal oxides, metal-containing ammonium salts,and organic-group-containing compounds are preferable, and halides,mineral acid salts, metal oxides, metal-containing ammonium salts, andorganic-group-containing compounds are more preferable. The abovecompounds may be used alone or in combination of two or more in arequired amount.

When the metal-containing compounds are attached to the carrier, themetal-containing compounds may be dissolved or dispersed in a solventand the resulting solutions and dispersion liquids may be used in any ofthe above attaching methods. The type of the solvent used in this stepis not limited and may be any type of solvent in which themetal-containing compounds can be dissolved or dispersed and which doesnot adversely affect the baking and hydrogen reduction of themetal-supporting material and the hydrogenation reaction in which thiscatalyst is used, which are conducted in the subsequent step. Examplesof the solvent include ketone solvents, such as acetone, alcoholsolvents, such as methanol and ethanol, ether solvents, such astetrahydrofuran and ethylene glycol dimethyl ether, and water. The abovesolvents may be used alone or in the form of a mixed solvent. Among theabove solvents, water is preferably used because water is inexpensiveand the solubility of the raw materials, that is, the metal-containingcompounds, in water is high.

When the metal-containing compounds are dissolved or dispersed in thesolvent, various additives may be optionally used in addition to thesolvent. For example, using a solution of carboxylic acid and/or acarbonyl compound may improve the dispersibility of each of the metalcomponents on the carrier which is achieved when the metal componentsare attached to the carrier, as described in Japanese Unexamined PatentApplication Publication No. 10-15366.

The metal-supporting material may be dried as needed. It is preferableto subject the metal-supporting material to a .reduction treatment stepafter the metal-supporting material has been dried and subsequentlybaked as needed, for the following reason: if the metal-supportingmaterial is subjected to the subsequent reduction treatment withoutbeing dried, the catalyst may have low reaction activity.

The method for drying the metal-supporting material is not limited andmay be any method capable of removing the solvent and the like used forattaching the metal components to the carrier. Normally, themetal-supporting material is dried in a stream of inert gas or at areduced pressure.

The pressure at which the metal-supporting material is dried is nor,limited. Normally, the metal-supporting material is dried at normalpressure or a reduced pressure.

The temperature at which the metal-supporting material is dried isnormally, but not limited to, 300° C. or less, is preferably 250° C. orless, is more preferably 200° C. or less, and is normally 80° C. ormore.

After the metal-supporting material has been dried, the metal-supportingmaterial may be baked as needed. Baking the metal-supporting materialincreases the likelihood of the catalyst having a high catalyticactivity and excellent reaction selectivity. The baking of themetal-supporting material may be performed in the air atmosphere. Forexample, the baking of the metal-supporting material may be performed byheating the metal-supporting material in an air stream at apredetermined temperature for a predetermined amount of time.

The temperature at which the metal-supporting material is baked isnormally, but not limited to, 100° C. or more, is preferably 250° C. ormore, is more preferably 400° C. or more, is normally 1000° C. or less,is preferably 700° C. or less, and is more preferably 600° C. or less.The amount of time during which the metal-supporting material is baked,which varies with the baking temperature, is normally 30 minutes ormore, is preferably 1 hour or more, is more preferably 2 hours or more,is normally 40 hours or less, is preferably 30 hours or less, and ismore preferably 10 hours or less.

<(ii) Reduction Treatment Step>

The metal-supporting material is normally subjected to a reductiontreatment using a reducing gas. In the reduction treatment, a publiclyknown method, such as liquid-phase reduction or a gas-phase reduction,may be used.

The reducing gas used in the reduction treatment step is not limited andmay be any gas having a reducing power. Examples of the reducing gasinclude hydrogen, methanol, and hydrazine. The reducing gas ispreferably hydrogen.

In the case where a hydrogen-containing gas is used as a reducing gas,the hydrogen concentration in the hydrogen-containing gas is notlimited. The hydrogen concentration in the hydrogen-containing gas maybe 100% by volume. Ir. another case, the hydrogen-containing gas may bediluted with an inert gas. The term “inert gas” used herein refers to agas unreactive with the metal-supporting material or a hydrogen ga3,such as nitrogen or water vapor. Normally, nitrogen is used as an inertgas. The hydrogen concentration in the reducing gas (hydrogen-containinggas) diluted with an inert gas is normally 5% by volume or more, ispreferably 15% by volume or more, is more preferably 30% by volume ormore, and is further preferably 50% by volume or more relative to theall the gas components. It is possible to use a hydrogen-containing gashaving a low hydrogen concentration at the initial stage of reductionand gradually increase the hydrogen concentration in thehydrogen-containing gas over the course of reduction.

The amount of time required for the reduction treatment, which varieswith the amounts of the metal-supporting material and the like that areto be treated and the type of the apparatus or the like used, isnormally 7 minutes or more, is preferably 15 minutes or more, is morepreferably 30 minutes or more, is normally 40 hours or less, ispreferably 30 hours or leas, and is more preferably 10 hours or less.The temperature at which the reduction treatment is performed isnormally 130° C. or more, is preferably 200° C. or more, is morepreferably 250° C. or more, is normally 700° C. or less, is preferably600° C. or less, and is more preferably 500° C. or less. If thereduction treatment is performed at an excessively high temperature, forexample the supported metal may b sintered and, consequently, theactivity of the. catalyst may be reduced.

In the reduction treatment, the reducing gas may be enclosed in thereactor or may be passed through the reactor. It is preferable to passthe reducing gas through the reactor. This is because passing thereducing gas through the reactor prevents the occurrence of localhydrogen deficiency. In the reduction treatment, water, ammoniumchloride, and the like may be produced as by-products in the rectordepending on the raw materials used, and the by-products may adverselyaffect the metal-supporting material that has not been subjected to thereduction treatment or the metal-supporting catalyst, which has beensubjected to the reduction treatment. Passing the reducing gas throughthe reactor enables the by-products to be discharged to the outside ofthe reaction system.

The amount of the reducing gas required by the reduction treatment isnot limited and may be set such that the objects of the first to thirdinventions are achieved. The amount of the reducing gas required by thereduction treatment can be set appropriately in accordance with theapparatus used, the size of the reactor used for reduction, the methodfor passing the reducing gas through the reactor, the method forfluidizing the catalyst, and the like.

The size of the metal-supporting catalyst, which has been subjected tothe reduction treatment, is net limited and basically the same as thesite of the carrier.

Examples of a preferable method for performing the reduction treatmentinclude a method in which the reducing gas is passed through themetal-supporting material with a fixed bed; a method in which thereducing gas is passed through the metal-supporting material that isdisposed to stand on a tray or a belt; and a method in which themetal-supporting material is caused to fluidize and the reducing gas ispassed through the fluidized metal-supporting material.

<(iii) Oxidative Stabilization Step>

In the production of this catalyst, as needed, the metal-supportingcatalyst, which is produced by reducing the metal-supporting material,is subjected to an oxidative stabilization treatment in order to controlthe oxidation state. Performing the oxidative stabilization treatmentenables the production of a catalyst that has excellent activity andexcellent selectivity and that can be handled in the air atmosphere.

The method for performing oxidative stabilization is not limited.Examples thereof include a method in which water is added to themetal-supporting catalyst, a method in which the metal-supportingcatalyst is charged into water, a method in which oxidativestabilization is performed using a gas having a low oxygen concentrationwhich is diluted with an inert gas, and a method in which stabilizationis performed using carbon dioxide. Among the above methods, the method.in which water is added to the metal-supporting catalyst, the method inwhich the metal-supporting catalyst is charged into water, and themethod in which oxidative stabilization is performed using the gashaving a low oxygen concentration are preferable, the method in whichoxidative stabilization (slow oxidation) is performed using the gashaving a low oxygen concentration (hereinafter, this method is referredto as “slow-oxidation method”) is more preferable, and a method in whichoxidative stabilization is performed in a stream of the gas having a lowoxygen concentration is particularly preferable.

The initial oxygen concentration with which oxidative stabilization isperformed using the gas having a low oxygen concentration is notlimited. The oxygen concentration with which the slew oxidation isstarted is normally 0.2% by volume or more, is preferably 0.5% by volumeor more, is normally 10% by volume or less, is preferably 8% by volumeor less, and is further preferably 7% by volume or less. If the oxygenconcentration is excessively lower than the lower limit, it takes aconsiderable amount of time to complete the oxidative stabilization andstabilization may fail to be achieved at a sufficient level. If theoxygen concentration is excessively higher than the upper limit, thetemperature of the catalyst may be excessively increased and thecatalyst may become deactivated.

The gas having a low oxygen concentration is preferably prepared bydiluting air with an inert gas. The inert, gas used for diluting air ispreferably nitrogen.

Examples of a method for performing the oxidative stabilization usingthe gas having a low oxygen concentration include a method in which thegas having a low oxygen concentration is passed through the catalystwith a fixed bed; a method in which the gas having a low oxygenconcentration is passed through the catalyst that is disposed to standon a tray or a belt; and a method in which the catalyst is caused tofluidize and the gas having a low oxygen concentration is passed throughthe fluidized catalyst.

The higher the dispersibility of the supported metal or. themetal-supporting catalyst, the higher the rate at which the oxidativestabilization is performed and the larger the amount of oxygen used inthe reaction. Therefore, the method in which the gas having a low oxygenconcentration is passed through the catalyst with a fixed bed and themethod in which the catalyst is caused to fluidize and the gas having alow oxygen concentration is passed through the fluidized catalyst arepreferable.

The method for producing this catalyst is not limited to theabove-described production method and may be any method capable ofproducing this catalyst. For example. the method for producing thiscatalyst nay include another publicly known step such that this catalystcan be produced.

[Production of Alcohol With This Catalyst]

This catalyst is suitable as a catalyst used in the reduction reaction(hydrogenation) of a carbonyl compound. An alcohol can be produced bytreating a carbonyl compound with this catalyst.

Preferable examples of the reduction reaction conducted with thiscatalyst include an alcohol production method which includes a step inwhich at least one carbonyl compound selected from the group consistingof a ketone, an aldehyde, a carboxylic acid, a carboxylic acid ester, acarboxylic acid amide, a carboxylic acid halide, and a carboxylicanhydride is reduced to produce an alcohol derived from the compound.Among the above compounds, a carboxylic acid can be directly reducedwith this catalyst to form an alcohol.

The carbonyl compound that is to be subjected to the reduction reactionnay be. any carbonyl compound that is industrially readily available.Specific examples of the carboxylic acid and/or the carboxylic acideater include aliphatic chain monocarboxylic acids, such as acetic acid,butyric acid, decancic acid, lauric acid, oleic acid, linoleic acid,linolenic acid, stearic acid, and palmitic acid; aliphatic cyclicmonocarboxylic acids, such as cyclohexanecarboxylic acid, naphthenicacid, and cyclopentanecarboxylic acid; aliphatic polycarboxylic acids,such as oxalic acid, malonic acid, succinic acid, methylsuccinic acid,glutaric acid, adipic acid, pimelic acid, suberic acid, sebacic acid,cyclohexanedicarboxylic acid, 1,2,4-butanetricarboxylic acid,1,3,4-cyclohexanetricarboxylic acid, bicyclohexyldicarboxylic acid, anddecahydronaphthalenedicarboxylic acid; aromatic carboxylic acids, suchas phthalic acid, isophthalic acid, terephthalic acid, and trimesicacid; carboxylic acids including a furan skeleton, such asfurancarboxylic acid and furandicarboxylic acid; carboxylic acid esters,such as methyl esters, ethyl esters, propyl esters, and butyl esters ofthe above carboxylic acids and esters of an alcohol produced by reducinga carboxylic acid; and lactones, such as γ-butyrolactone,δ-valerolacton(r), and ε-caprolactone.

Specific examples of the carboxylic acid amide include methyl amides andethyl amides of the above carboxylic acids.

Specific examples of the carboxylic acid halide include chlorides andbromides of the above carboxylic acids.

Specific examples of the carboxylic anhydride include acetic anhydride,succinic anhydride, maleic anhydride, and phthalic anhydride.

Examples of the aldehyde and the ketone include benzaldehyde,propionaldehyde, acetaldehyde, 3-hydroxypropionaldehyde, furfural,hydroxymethylfurfural, acetone, benzophenone, glucose, xylose, lactose,and fructose.

The carboxylic acid and carboxylic acids constituting the carboxylicacid ester, the carboxylic acid amide, the carboxylic acid halide,and/or the carboxylic anhydride are preferably, but not limited to,chain or cyclic saturated aliphatic carboxylic acids, are morepreferably carboxylic acids a portion of which excluding carboxyl groupshas 20 or less carbon atoms. The number of the carbon atoms included inthe carboxylic acids is more preferably 14 or less.

In the present invention, among the above carbonyl compounds that are tobe subjected to the reduction reaction, the carboxylic acid, thecarboxylic acid ester, the carboxylic anhydride, and the aldehyde arepreferable, the carboxylic acid, the carboxylic acid ester, thecarboxylic anhydride, and the aldehyde are more preferable, and thecarboxylic acid arid the carboxylic acid ester are particularlypreferable from the viewpoint of ease of availability of the rawmaterials. However, the carbonyl compounds that are to be subjected tothe reduction reaction are not limited to the above carbonyl compounds.

The carboxylic acid is preferably a dicarboxylic acid and is furtherpreferably a dicarboxylic acid represented by Formula (1) below theportion of which except carboxyl groups includes 20 or less carbonatoms.

HOOC—R¹—COOH   (2)

(in Formula (1), R¹ represents an aliphatic or alicyclic hydrocarbongroup that may have a substituent, the portion of the hydrocarbon groupexcept the substituent including 1 to 20 carbon atoms)

This catalyst enables a polyvalent carboxylic acid, such as the abovedicarboxylic acid, to be converted into a correspondinghydroxycarboxylic acid, lactone, or polyhydric alcohol with highselectivity at a high yield. Appropriately selecting the productionconditions, 3uch as the type of catalyst used, the reaction pressure,the reaction temperature, and the amount of time the raw materials areretained, enables the ratio between the amount of the hydroxycarboxylicacid or lactone produced and the amount, of the polyhydric alcoholproduced to be controlled.

Other examples of particularly preferable carbonyl compounds includecarboxylic acids having a furan skeleton which are derived from biomassresources, such as furandicarboxylic acid, and aldehydes, such ashydroxymethylfurfural.

Although the reduction reaction using this catalyst may be conducted ina liquid phase or gas phase, the reduction reaction using this catalystis preferably conducted in a liquid phase. Although the reductionreaction using this catalyst in a liquid phase may be conducted withoutusing a solvent or in the presence of a solvent, the reduction reactionusing this catalyst in a liquid phase is normally conducted in thepresence of a solvent.

Examples of the solvent include, normally, water; lower alcohols, suchas methanol and ethanol; alcohols that are the reaction products;ethers, such as tetrahydrofuran, dioxane, and ethylene glycol dimethylether; and hydrocarbons, such as hexane, decalin, and methylcyclohexane.The above solvents may be used alone or in a mixture of two or more.

In particular, in the case where a carbonyl compound is to foe reduced,it is preferable to use a water solvent from the viewpoints ofsolubility and the like. The amount, of the solvent used is normally,but not limited to, about 0.1 to 20 times by mass, is preferably 0.5 to10 times by mass, and is more preferably about 1 to 10 times by mass theamount of the carbonyl compound used as a raw material.

The reduction reaction using this catalyst is normally conducted in apressurized hydrogen gas. The reaction is normally conducted at 100° C.to 300° C. and is preferably conducted at 120° C. to 250° C. Thereaction pressure is normally 1 to 30 MPaG, .is preferably 1 to 25 MPaG,and is further preferably 5 to 25 MPaG.

After the reaction has been terminated, the product of the reductionreaction using this catalyst is normally recovered by solventdistillation, solvent distillation followed by extraction using anorganic solvent, distillation, sublimation, crystallization,chromatography, or the like, which depends on the physical properties ofthe product. In the case where the product is liquid at handlingtemperature, it is preferable to recover the product, while purifyingthe product by distillation. In the case where the product is solid athandling temperature, it is preferable to recover the product whilepurifying the product by crystallization. It is preferable to purify thesolid product by washing.

EXAMPLES

The present invention is described below further in detail withreference to Examples. The present invention is not limited by Examplesbelow without departing from the scope of the present invention.

(Measurement of Sulfate Ion Content)

A 0.2 M-aqueous sodium hydroxide solution was added to the sample. Theresulting mixture was irradiated with ultrasonic wave and subsequentlysubjected to centrifugal separation. The resulting liquid was analyzedby ion chromatography in order to determine the content of sulfate ionsin the sample.

(Measurement of Sulfur Content)

The content, of sulfur in the sample was determined in accordance with ahigh-frequency furnace combustion-infrared detection method (carbonsulfur analyzer) by combusting the sample in a high-frequency inductionheating furnace under an oxygen atmosphere and calculating the contentof sulfur in the combustion gas by an infrared detection method.

Examples and Comparative Examples of First Invention Example I-1

Ammonium perrhenate and tetraethoxygermanium(IV) were dissolved inwater. Titanium oxide particles (Catalysis Society of Japan, Referencecatalyst JRC-TIO-14 produced by Ishihara Sangyc Kaisha, Ltd.) having aspecific surface area of 308 m²/g were added to the resulting solution.The solution was stirred at room temperature for 20 minutes.Subsequently, water was removed using an evaporator. Then, drying wasperformed at 100° C. for 4 hours. The resulting material was chargedinto a vertical baking tube. While air was passed through the tube, abaking treatment was performed at 500° C. for 3 hours. The resultingsolid was charged into a vertical baking tube. While a hydrogen gas waspassed through the tube, a reduction treatment was performed at 500° C.for 30 minutes. Subsequently, the temperature was reduced to 30° C.After purging with an argon gas had been performed, a 6-volume %oxygen/nitrogen gas was passed through the tube. Hereby, 5% rhenium-5%germanium/titanium oxide catalyst particles having stabilized surfaces(the ratio of the amount of rhenium supported to the total mass of thecatalyst: 5 mass %, the ratio of the amount of germanium supported tothe total mass of the catalyst: 5 mass % (Ge/Re=1)) were prepared. Thesulfate ion contents in the titanium oxide particles (Catalysis societyof Japan, Reference catalyst JRC-TIO-14) and the catalyst were 0.2% bymass and 0.14% by mass, respectively. The sulfur content in the catalystwas 0.078% by mass.

Into a 70-mL high-pressure reactor, 100 mg of the catalyst prepared bythe above method, 500 mg of sebacic acid, 2 g of water, and a stirrerchip were charged. After the reactor had been purged with nitrogen, ahydrogen gas (7 MPaG) was introduced into the reactor at roomtemperature. Subsequently, a hydrogenation reaction was conducted at220° C. for 7.5 hours. The reaction pressure at 220° C. was 13 MPaG.After the reaction had beer, terminated, the temperature was reduced toroom temperature and the pressure was then reduced. An analysis of thereaction liquid by gas chromatography confirmed that the molar yields of1,10-decanediol and 10-hydroxydecanoic acid in the reaction were 5.9%and 48.1%, respectively, and the molar ratio of the by-products(1-nonanol, 1-aecanol, 1-nonanoic acid, and 1-decanoic acid) to thetarget components (1,10-decanediol and 10-hydroxydecancic acid) was0.016.

Example I-2

A hydrogenation reaction was conducted as in Example I-1 with thecatalyst prepared in Example I-1, except that the amount of time duringwhich the hydrogenation reaction was conducted was changed to 18 hours.The molar yields of 1,10-decanediol and 10-hydroxydecanoic acid in thereaction were 89.3% and 6.5%, respectively. The molar ratio of theby-products (1-nonanol, 1-decanol, 1-nonanoic acid, and 1-decanoic acid)to the target components (1,10-decanediol and 10-hydroxydecanoic acid)was 0.017.

Example I-3

A hydrogenation reaction was conducted as in Example I-1 with a catalystprepared as in Example I-3, except that the treatment in which thesurfaces of the catalyst particles were stabilized by passing a 6-volume% oxygen/nitrogen gas through the tube was not performed after thereduction treatment had been performed while a hydrogen gas was passedthrough the tube. The molar yields of 1,10-decanediol and10-hydroxydecancic acid in the reaction were 74.7% and 2.6%,respectively. The molar ratio of the by-products (1-nonanol, 1-decanol,1-nonanoic acid, and 1-decanoic acid) to the target components(1,10-decanediol and 10-hydroxydecanoic acid) was 0.004.

Example I-4

A 5% rhenium-5% germanium/titanium oxide catalyst was prepared by thesame catalyst preparation method as in Example I-1, except that thetitanium oxide particles were changed to titanium oxide particles havinga specific surface area of 302 m²/g and a sulfate ion content of 4.8% bymass (MC-150, produced by Ishihara Sangyo Kaisha, Ltd.). The sulfate ioncontent in the catalyst was 0.63% by mass. The sulfur content in thecatalyst was 0.57% by mass. A hydrogenation reaction was conducted as inExample I-1 with this catalyst. The molar yields of 1,10-decanediol and10-hydroxydecanoic acid in the reaction were 81.7% and 0.6%,respectively. The molar ratio of the by-products (I-nonanol, 1-decanol,1-nonanoic acid, and 1-decanoic acid) to the target, components(10-hydroxydecanoic acid and 1,10-decanediol) was 0.006.

Example I-5

A 5% rhenium-5% germanium/titanium oxide catalyst was prepared by thesame method as in Example I-1. except that the titanium oxide particleswere changed to titanium oxide particles having a specific surface areaof 90 m²/g and a sulfate ion content of 3.6% by mass (MC-90, produced byIshihara Sangyo Kaisha, Ltd.). The sulfate ion content in the catalystwas 0.30% by mass. The sulfur content in the catalyst was 0.35% by mass,A hydrogenation reaction was conducted as in Example I-1 with thiscatalyst. The molar yields of 1,10-decanodiol and 10-hydroxydecanoicacid in the reaction were 4.5% and 36.8%, respectively. The molar ratioof the by-products (1-nonanol, 1-decanol, 1-nonanoic acid, and1-decanoic acid) to the target components (10-hydroxydecanoic acid and1,10-decanediol) was 0.011.

Example I-6

A 5% rheniuns-5% indium/titanium, oxide catalyst, was prepared by thesame catalyst preparation method as in Example I-1, except thatindium(III) chloride tetrahydrate was used instead oftetraethoxygermanium(IV). Subsequently, a hydrogenation reaction wasconducted as in Example I-1. The molar yields of 1,10-decanediol and10-hydroxydecanoic acid in the reaction were 9.0% and 43.5%,respectively. The molar, ratio of the by-products (1-nonanol, 1-decanol,1-nonanoic acid, and 1-decanoic acid) to the target, components10-hydroxydecanoic acid and 1,10-decanediol) was 0.034.

Example I-7

A 5% rheniuns-5% silicon/titanium oxide catalyst was prepared by thesame catalyst preparation method as in Example I-1, except thattetraethoxysilane(IV) was used instead of tetraethoxygermanium(IV) andethanol was used instead of water for preparing the solution.Subsequently, a hydrogenation reaction was conducted as in Example I-1.The molar yields or 1,10-decanediol and 10-hydroxydecanoic acid in thereaction were 1.7% and 23.1%, respectively. The molar ratio of theby-products (1-nonanol, 3-docanol, 1-nonanoic acid, and 1-decanoic acid)to the target components (10-hydroxydecanoic acid and 1,10-decanediol)was 0.039.

Example I-8

A 5% rhenium-1% germanium/titanium oxide catalyst was prepared by thesame catalyst preparation method as in Example I-1, except that theratio between the amounts of ammonium perrhenate andtetraethoxygermanium(IV) used as metal raw materials was changed and thesurfaces of the catalyst particles were not stabilized by passing the6-volume % oxygen/nitrogen gas through the tube subsequent to thereduction treatment. A hydrogenation reaction was conducted as inExample I-1 with this catalyst, except that the amount of time duringwhich the reaction was conducted was changed to 3 hours. The molaryields of 1,10-decanediol and 10-hydroxydecanoic acid in the reactionwere 38.7% and 10.8%, respectively. The moinr ratio of the by-products(1-nonanol, 1-decanol, 1-nonanoic acid, and 1-decanoic acid) to thetarget components (10-hydroxydecanoic acid and 1,10-decanediol) was0.009.

Example I-9

A hydrogenation reaction was conducted with the catalyst prepared inExample I-3 as in Example I-1, except that the amount of time duringwhich the reaction was conducted was changed to 3 hours. The molaryields of 1,10-docanediol and 10-hydroxydecanoic acid in the reactionwere 35.3% and 32.9%, respectively. The molar ratio of the by-products(1-nonanol, 1-decanol, 1-nonanoic acid, and 1-decanoic acid) to thetarget components (10-hydraxydecanoic acid and 1,10-decanediol) was0.005.

Example I-10

A 5% rheniuns-5% germanium-0.5% ruthenium/titanium oxide catalyst wasprepared by the same catalyst preparation method as in Example I-1,except that ammonium perrbenate, tetraethoxygermanium(IV), andruthenium(III) chloride were used as metal raw materials and thesurfaces of the catalyst particles were not stabilized by passing the6-volume % oxygen/nitrogen gas through the tube subsequent to thereduction treatment. Subsequently, a hydrogenation reaction wasconducted as in Example I-1. The molar yields of 1,10-decanediol and10-hydroxydecancic acid in the reaction were 72.0% and 3.6%,respectively. The molar ratio of the by-products (1-nonanol, 1-decanol,1-nonanoic acid, and 1-decanoic acid) to the target components(10-hydroxydecanoic acid and 1,10-decanediol) was 0.006.

Example I-11

A 5% rhenium-5% germaniunt-5% ruthenium/titanium oxide catalyst wasprepared by the same catalyst preparation method as in Example I-10,except that the ratio between the amounts of ammonium perrhenate,tetraethoxygermanium(IV), and ruthenium(III) chloride used as metal rawmaterials was changed. Subsequently, a hydrogenation reaction wasconducted as in Example I-1. The molar yields of 1,10-decanediol and10-hydroxydecanoic acid in the reaction were 89.0% and 0.4%,respectively. The molar ratio of the by-products (1-nonanol, 1-decanol,1-nonanoic acid, and 1-decanoic acid) to the target components(10-hydroxydecanoic acid and 1,10-decanediol) was 0.020.

Comparative Example I-1

A 5% rhenium/titanium oxide catalyst was prepared by the same catalystpreparation method as in Example I-1, except that tetraethoxygermaniumwas not used. Subsequently, a hydrogenation reaction was conducted as inExample I-1. The molar yields of 1,10-decanediol and 10-hydroxydecanoicacid in the reaction were 0.1% and 21.0%, respectively. The molar, ratioof the by-products (1-nonanol, 1-decanol, 1-nonanoic acid, and1-decanoic acid) to the target components (1,10-decanediol and10-hydroxydecanoic acid) was 0.060.

Comparative Example I-2

A 5% rhenium-5% palladium/titanium oxide catalyst was prepared by thesame catalyst preparation method as in Example X-1, except that ammoniumperrhenate and dichlorotetraamminepalladium(II) were used as metal rawmaterials. Subsequently, a hydrogenation reaction was conducted as inExample I-1. The molar yields of 1,10-decanediol and 10-hydroxydecanoicacid in the reaction were 33.1% and 0.0%, respectively. The molar ratioof the by-products (1-nonanol, 1-decanol, 1-nonanoic acid, and1-decanoic acid) to the target components (10-hydroxydecanoic acid and1,10-decanediol) was 0.325.

Comparative Example I-3

A 5% rhenium-5% ruthenium/titanium oxide catalyst was prepared by thesame catalyst preparation method as in Example I-3, except that ammoniumperrhenate and ruthenium(III) chloride were used as metal raw materials.Subsequently, a hydrogenation reaction was conducted as in Example I-1.The molar yields of 1,10-decanediol and 10-hydroxydecanoic acid in thereaction were 45.0% and 11.1%, respectively. The molar ratio of theby-products (1-nonanol, 1-decanol, 1-nonanoic acid, and 1-decanoic acid)to the target components (10-hydroxydecanoic acid and 1,10-decanediol)was 0.063.

Table 1 summarizes the results obtained in Examples I-1 to I-11 andComparative examples I-1 to I-3.

TABLE 1 Reaction results Hydrogenation Yield of 1,10- Yield of 10-By-product/target reaction time decanediol hydroxydecanoic componentmolar Catalyst (hour) (mol %) acid (mol %) ratio Example 5%Re ·5%Ge/TiO₂ 7.5 5.9 48.1 0.016 I-1 Example 5%Re · 5%Ge/TiO₂ 18 89.3 6.50.017 I-2 Example 5%Re · 5%Ge/TiO₂ 7.5 74.7 2.6 0.004 I-3 Example 5%Re ·5%Ge/TiO₂ 7.5 81.7 0.6 0.006 I-4 Example 5%Re · 5%Ge/TiO₂ 7.5 4.5 36.80.011 I-5 Example 5%Re · 5%In/TiO₂ 7.5 9.0 43.5 0.034 I-6 Example 5%Re ·5%Si/TiO₂ 7.5 1.7 23.1 0.039 I-7 Example 5%Re · 1%Ge/TiO₂ 3 38.7 10.80.009 I-8 Example 5%Re · 5%Ge/TiO₂ 3 35.3 32.9 0.005 I-9 Example 5%Re ·5%Ge · 7.5 72.0 3.6 0.006 I-10 5%Ru/ TiO₂ Example 5%Re · 5%Ge · 7.5 89.00.4 0.020 I-11 5%Ru/ TiO₂ Comparative 5%Re/TiO₂ 7.5 0.1 21.0 0.060example I-1 Comparative 5%Re · 5%Pd/TiO₂ 7.5 33.1 0.0 0.825 example I-2Comparative 5%Re · 5%Ru/TiO₂ 7.5 45.0 11.1 0.063 example I-3

Example I-12

Ammonium perrhenate and tetraethoxygexmanium(XV) were dissolved inwater. Titanium oxide particles (MC-150, produced by Ishih&ra SangyoKaisha, Ltd.>having a specific surface area of 302 m²/g and a sulfateion content of 4.8% by mass were added to the resulting solution. Thesolution was stirred at room temperature for 20 minutes.

Subsequently, water was removed using an evaporator. Then, drying wasperformed at 100° C. for 4 hours. The resulting material was chargedinto a vertical baking tube, while air was passed through the tube, abaking treatment was performed at 500° C. for 3 hours. The resultingsolid was charged into a vertical baking tube. While a hydrogen gas waspassed through the tube, a reduction treatment was performed at 500° C.for 30 minutes. Hereby, a 5% rhenium-5% germanium/titanium oxidecatalyst (the ratio of the amount of rhenium supported to the total massof the catalyst: 5 mass %, the ratio of the amount of germaniumsupported to the total mass of the catalyst: 5 mass % (Ge/Re=1)) wasprepared.

Into a 70-mL high-pressure reactor, 70 mg of the catalyst prepared bythe above method, 260 mg of decanoic acid, 1.2 mL of methanol, and astirrer chip were charged. After the reactor had been purged withnitrogen, a hydrogen gas (7 MPaG) was introduced into the reactor atroom temperature. Subsequently, a hydrogenation reaction -was conductedat 220° C. for 3 hours. The reaction pressure at 220° C. was 13 MPaG.After the reaction had been terminated, the temperature was reduced toroom temperature and the pressure was then reduced. An analysis of thereaction liquid by gas chromatography confirmed that the molar yield of10-decanol in the reaction was 76.5% and the molar ratio of theby-products (nonane and decane) to the target component (10-decanol) was0.004.

Example I-13

A 5% rheniura-5% germanium/zirconium oxide catalyst was prepared by thesame catalyst preparation method as in Example I-6, except thatzirconium oxide particles having a specific surface area of 97 m²/gwhich did not include a sulfate ion was used instead of the titaniumoxide particles. Subsequently, a hydrogenation reaction was conducted asin example I-8, except that a water solvent was used instead ofmethanol. The molar yield of 10-decanol in the reaction was 23.2% andthe molar ratio of the by-products (nonane and decane) to the targetcomponent (10-decanol) was 0.001.

A comparison between the results obtained in Examples I-1 to I-11 andthe results obtained in Comparative examples I-1 to I-3, where acatalyst including a carrier composed of titanium oxide was used,confirms that using a catalyst produced by attaching the specific secondcomponent to a catalyst including rhenium and an oxide of a metalbelonging to Group 4 of the periodic table increases the total amount of1,10-decanediol and 10-hydroxydecanoic acid produced in a hydrogenationreaction of a earboxylic acid per unit specific surface area andenhances catalytic activity. Furthermore, the occurrence of sidereactions, such as a defunctionalization reaction associated withdehydration and hydrogenation, can fee markedly reduced. Theadvantageous effects become significant particularly when a catalystincluding germanium is used. Note that, the total amount of1,10-decanediol and 10-hydroxydecanoic acid produced is used as ameasure of catalytic activity because 10-hydroxydecancic acid isconsidered a reaction intermediate of the 1,10-decanediol product andcan be derived into 1,10-decanediol when the reaction time is furtherprolonged. A comparison between the results obtained in Examples I-12and I-13 confirms that a catalyst including a carrier composed ofzirconium oxide also has the same advantageous effects as a catalystincluding a carrier composed of titanium oxide. Specifically, it isconfirmed that a catalyst including a zirconium oxide carrier has acatalytic activity comparable to that of a catalyst including a titaniumoxide carrier in terms of catalytic activity per unit specific surfacearea. A comparison between the results obtained in Examples I-1 and I-2confirms that reaction selectivity car. be maintained by using acatalyst that includes germanium even under high-inversion-rate reactionconditions, which have been an issue for rhenium catalysts. In addition,a comparison between the results obtained in Examples I-1, I-4, and I-5confirms that the higher the sulfate ion content in the catalyst, thehigher the degree of reduction in the defunctionalization reaction, thehigher the reaction selectivity, and the higher the degree of increasein the catalytic activity of the hydrogenation catalyst per unitspecific surface area of the carrier. The remarkable reduction in theside reactions enables the production of an alcohol with a high purityand a reduction in the costs of purification of the alcohol produced.

Examples and Comparative Examples of Second Invention Example II-1

Ammonium perrnenate and tetraethoxygermanium(IV) were dissolved inwater. Titanium oxide particles (Catalysis Society of Japan, Referencecatalyst JRC-TIO-14 produced by Ishihare Sangyo Kaisha, Ltd.) having aspecific surface area of 308 m²/g were added to the resulting solution.The solution was stirred at room temperature for 20 minutes.Subsequently, water was removed using an evaporator. Then, drying wasperformed at 100° C. for 4 hours. The resulting material was chargedinto a vertical baiting tube. While air was passed through the tube, abaking treatment was performed at 500° C. for 3 hours. The resultingsolid was charged into a vertical baking tube. While a hydrogen gas waspassed through the tube, a reduction treatment was performed at 500° C.for 30 minutes. Subsequently, the temperature was reduced to 30° C.After purging with an argon gas had been performed, a 6-volume %oxygen/nitrogen gas was passed through the tube. Hereby, 5% rhenium-5%germanium/titanium oxide catalyst particles having stabilized surfaces(the ratio of the amount of rhenium supported to the total mass of thecatalyst: 5 mass %, the ratio of the amount of germanium supported tothe total mass of the catalyst: 5 mass % (Ge/Re=1)) were prepared. Thesulfate ion contents in the titanium oxide particles (Catalysis Societyof Japan, Reference catalyst JRC-TIO-14) and the catalyst were 0.2% bymass and 0.14% by mass, respectively. The sulfur content in the catalystwas 0.078% by mass.

Into a 70-mL high-pressure reactor, 100 mg of the catalyst prepared bythe above method, 500 mg of sebacic acid, 2 g of water, and a stirrerchip were charged. After the reactor had been purged with nitrogen, ahydrogen gas (7 MPaG) was introduced into the reactor at roomtemperature. Subsequently, a hydrogenation reaction was conducted at220° C. for 7.5 hours. The reaction pressure at. 220° C. was 13 MPaG.After the reaction had been terminated, the temperature was reduced toroom temperature and the pressure was then reduced. An analysis of thereaction liquid by gas chromatography confirmed that the molar yields of1,10-decanediol and 10-hydroxydecanoic acid in the reaction were 5.9%and 48.1%, respectively, and the molar ratio of the by-products(1-nonanol, 1-decanol, 1-nonanoic acid, and 1-decanoic acid) to thetarget components (1,10-decandiol and 10-hydroxydecanoic acid) was0.016.

Example II-2

A hydrogenation reaction was conducted as in Example II-1 with thecatalyst prepared in Example II-1, except that the amount of time duringwhich the hydrogenation reaction was conducted was changed to 18 hours.The molar yields or 1,10-decanediol and 10-hydroxydecanoic acid in thereaction were 89.3% and 6.5%, respectively. The molar ratio of theby-products (1-nonanol, 1-decanol, 1-nonanoic acid, and 1-decanoic acid)to the target components (1,20-decanediol and 10-hydroxydecanoic acid)was 0.017.

Example II-3

A hydrogenation reaction was conducted as in Example II-1 with acatalyst prepared as in Example II-1, except that the treatment in whichthe surfaces of the catalyst particles were stabilized by passing a6-volume % oxygen/nitrogen gas through the tube was not performed afterthe reduction treatment had been performed while a hydrogen gas waspassed through the tube. The molar yields of 1,10-docanediol and10-hydroxydecanoic acid in the reaction wore 74.7% and 2.6%,respectively. The molar ratio of the by-products (1-nonanol, 1-decanol,1-nonanoic acid, and 1-decanoic acid) to the target components(1,10-decanediol and 10-hydroxydecanoic acid) was 0.004.

Example II-4

A 5% rhenium-5% germanium/titanium oxide catalyst was prepared by thesame catalyst preparation method as in Example II-1, except that thetitanium oxide particles were changed to titanium oxide particles havinga specific surface area of 302 m²/g and a sulfate ion content of 4.8% bymass (MC-150, produced by Ishihara Sangyo Kaisha, Ltd.). The sulfate ioncontent in the catalyst was 0.63% by mass. The sulfur content in thecatalyst was 0.57% by mass, a hydrogenation reaction was conducted as inExample II-1 with this catalyst. The molar yields of 1,10-decanediol and10-hydroxydecanoic acid in the reaction were 81.7% and 0.6%,respectively. The molar ratio of the by-products (1-nonanol, 1-decanol,1-nonanoic acid, and 1-decanoic acid) to the target components(10-hydroxydecanoic acid and 1,10-decanediol) was 0.006.

Example II-5

A 5% rhenium-5% germanium/titanium oxide catalyst was prepared by thesame method as in Example II-1, except that the titanium oxide particleswere changed to titanium oxide particles having a specific surface areaof 90 m²/g and a sulfate ion content of 3.6% by mass (MC-90, produced byIshihare Sangyo Kaisha, Ltd.). The sulfate ion content in the catalystwas 0.30% by mass. The sulfur content in the catalyst was 0.35% by mass.A hydrogenation reaction was conducted as in Example II-1 with thiscatalyst. The molar yields of 1,10-decanedioi and 10-hydroxydecanoicacid in the reaction were 4.5% and 36.8%, respectively. The molar ratioof the by-products (1-nonanol, 1-decanol, 1-nonanoic acid, and1-decanoic acid) to the target components (10-hydroxyclecanoic acid and1,10-decanediol) was 0.011.

Example II-6

A 5% rhenium-5% indium/titanium oxide catalyst was prepared by the samecatalyst preparation method as in Example II-1, except, that indium(III)chloride tetrahydrate was used instead of tetraethoxygermanium(IV).Subsequently, a hydrogenation reaction was conducted as in Example II-1.The molar yields of 1,10-decanediol and 10-hydroxydecanoic acid in thereaction were 9.0% and 43.5%, respectively. The molar ratio of theby-products (1-nonanol, 1-decanol, 1-nonanoic acid, and 1-decaroic acid)to the target components (10-hydroxydecanoic acid and 1,10-decanediol)was 0.034.

Example II-7

A 5% rhenium-5% silicon/titanium oxide catalyst was prepared by the samecatalyst preparation method as in Example II-1, except thattetraethoxysilane(IV) was used instead of tetraethoxygermanium(IV) andethanol was used instead of water for preparing the solution.Subsequently, a hydrogenation reaction was conducted as in Example II-1.The molar yields of 1,10-decarediol and 10-hydroxydecanoic acid in thereaction were 1.7% and 23.1%, respectively. The molar ratio of theby-products (1-nonanol, 1-decanol, 1-nonanoic acid, and 1-decanoic acid)to the target components (10-hydroxydecanoic acid and 1,10-decanediol)was 0.039.

Example II-6

A 5% rhenium-1% germanium/titanium oxide catalyst was prepared by thesame catalyst preparation method as in Example II-1, except that theratio between the amounts of ammonium perrhenate andtetraethoxygermanium(IV) used as metal raw materials was changed and thesurfaces of the catalyst particles were not stabilized by passing the6-volume % oxygen/nitrogen gas through the tube subsequent to thereduction treatment. A hydrogenation reaction was conducted as inExample II-1 with this catalyst, except that the amount of time duringwhich the reaction was conducted was changed to 3 hours. The molaryields of 1,10-decanediol and 10-hydroxydecanoic acid in the reactionwere 36.7% and 10.8%, respectively. The molar ratio of the by-products(1-nonanol, 1-decanol, 1-nonanoic acid, and 1-decanoic acid) to thetarget components (10-hydroxydecanoic acid and 1,10-docanediol) was0.009.

Example II-9

A hydrogenation reaction was conducted with the catalyst prepared inExample 11-3 as in Example II-1, except that the amount of time duringwhich the reaction was conducted was changed to 3 hours. The molaryields of 1,10-decanediol and 10-hydroxydecanoic acid in the reactionwere 35.3% and 32.9%, respectively. The molar ratio of the by-products(1-nonanol, 1-decanol, 1-nonanoic acid, and 1-decanoic acid) to thetarget components (10-hydroxydecanoic acid and 1,10-decanediol) was0.005.

Example II-10

A 5% rhenium-5% germanitxm-0.5% ruthenium/titanium oxide catalyst wasprepared by the same catalyst preparation method as in Example II-1,except that ammonium perrhenate, tetraethoxygermanium(IV), andruthenium(III) chloride were used as metal raw materials and thesurfaces of the catalyst particles w-re not stabilized by passing the6-volume % oxygen/nitrogen gas through the tube subsequent to thereduction treatment. Subsequently, a hydrogenation reaction wasconducted as in Example II-1. The molar yields of 1,10-decanediol and10-hydroxydecanoic acid in the reaction were 72.0% and 3.6%,respectively. The molar ratio of the by-products (1-nonanol, 1-decanol,1-norsanoic acid, and 1-decanoic acid) to the target, components(10-bydroxydecanoic acid and 1,10-decanediol) was 0.006.

Example II-11

A 5% rhenium-5% germanium-5% ruthenium/titanium oxide catalyst wasprepared by the same catalyst preparation method as in Example II-10,except that the ratio between the amounts of ammonium perrhenate,tetraethoxygermanium(XV) and ruthenium(III) chloride used as metal rawmaterials was changed. Subsequently, a hydrogenation reaction wasconducted as in Example II-1. The molar yields of 1,10-decanediol and10-hydroxydecanoic acid in the reaction wore 39.0% and 0.4%,respectively. The molar ratio of the by-products (1-nonanol, 1-decanol,1-nonanoic acid, and 1-decanoic acid) to the target components(10-hydroxydecanoic acid and 1,10-decanediol) was 0.020.

Comparative Example II-1

A 5% rhenium/titanium oxide catalyst was prepared by the same catalystpreparation method as in Example II-1, except chat tetraethoxygermaniumwas not used. Subsequently a hydrogenation reaction was conducted as inExample II-1. The molar yields of 1,10-decanediol and 10-hydroxydecanoicacid in the reaction were 0.1% and 21.0%, respectively. The molar ratioof the by-products (1-nonanol, 1-decanol, 1-nonanoic acid, and1-decanoic acid) to the target components (1,10-decanediol and10-hydroxydecanoic acid) was 0.060.

Comparative Example II-2

A 5% rhenium-5% palladium/titanium oxide catalyst was prepared by thesame catalyst preparation method as in Example II-1, except thatammonium perrhenate and dichlorotetraanuninepalladium(II) were used asmetal raw materials. Subsequently, a hydrogenation reaction wasconducted as in Example I-1. The molar yields of 1,10-decanediol and10-hydroxydecanoic acid m the reaction were 33.1% and 0.0%,respectively. The molar ratio of the by-products (1-nonanol, 1-decanol,1-nonanoic acid, and 1-decanoic acid) to the target components(10-hydroxydecanoic acid and 1,10-decanediol) was 0.825.

Comparative Example II-3

A 5% rhenium-5% ruthenium/titanium oxide catalyst was prepared by thesame catalyst preparation method as in Example II-1, except thatammonium perrhenate and ruthenium (III) chloride were used as metal, rawmaterials. Subsequently, a hydrogenation reaction was conducted as inExample II-1. The molar yields of 1,10-decanediol and 10-hydroxydecanoicacid in the reaction were 45.0% and 11.1%, respectively. The molar ratioof the by-products (1-nonanol, 1-decanol, 1-nonanoic acid, and1-decanoic acid) to the target components (10-hydroxydecanolc acid and1,10-decanediol was 0.063.

Table 2 summarizes the results obtained in Examples II-1 to II-11 andComparative examples II-1 to II-3.

TABLE 2 Reaction results Hydrogenation Yield of 1,10- Yield of 10-By-product/target reaction time decanediol hydroxydecanoic componentmolar Catalyst (hour) (mol %) acid (mol %) ratio Example 5%Re ·5%Ge/TiO₂ 7.5 5.9 48.1 0.016 II-1 Example 5%Re · 5%Ge/TiO₂ 18 89.3 6.50.017 II-2 Example 5%Re · 5%Ge/TiO₂ 7.5 74.7 2.6 0.004 II-3 Example 5%Re· 5%Ge/TiO₂ 7.5 81.7 0.6 0.006 II-4 Example 5%Re · 5%Ge/TiO₂ 7.5 4.536.8 0.011 II-5 Example 5%Re · 5%In/TiO₂ 7.5 9.0 43.5 0.034 II-6 Example5%Re · 5%Si/TiO₂ 7.5 1.7 23.1 0.039 II-7 Example 5%Re · 1%Ge/TiO₂ 3 38.710.8 0.009 II-8 Example 5%Re · 5%Ge/TiO₂ 3 35.3 32.9 0.005 II-9 Example5%Re · 5%Ge · 7.5 72.0 3.6 0.006 II-10 5%Ru/ TiO₂ Example 5%Re · 5%Ge ·7.5 89.0 0.4 0.020 II-11 5%Ru/ TiO₂ Comparative 5%Re/TiO₂ 7.5 0.1 21.00.060 example II-1 Comparative 5%Re · 5%Pd/TiO₂ 7.5 33.1 0.0 0.825example II-2 Comparative 5%Re · 5%Ru/TiO₂ 7.5 45.0 11.1 0.063 exampleII-3

Example II-12

Ammonium perrhenate and tetraethoxygermanium(IV) were dissolved inwater. Titanium oxide particles (MC-150, produced by Ishihara SangyoKalsha, Ltd.) having a specific surface area of 302 m²/g and a sulfateion content of 4.8% by mass were added to the resulting solution. Thesolution was stirred at room temperature for 20 minutes.

Subsequently, water was removed using an evaporator. Then, drying wasperformed at 100° C. for 4 hours. The resulting material was chargedinto a vertical baking tube, while air was passed through the tube, abaking treatment was performed at 500° C. for 3 hours. The resultingsolid was charged into a vertical baking tube. While a hydrogen gas waspassed through the tube, a reduction treatment was performed at 500° C.for 30 minutes. Hereby, a 5% rhenium-5% germanium/titanium oxidecatalyst (the ratio of the amount of rhenium supported to the total massof the catalyst: 5 mass %, the ratio of the amount of germaniumsupported to the total mass of the catalyst: 5 mass % (Ge/Re=1)) wasprepared.

Into a 70-mL high-pressure reactor, 70 mg of the catalyst prepared bythe above method, 260 mg of decanoic acid, 1.2 mL of methanol, and astirrer chip were charged. After the reactor had been purged withnitrogen, a hydrogen gas (7 MPaG) was introduced into the reactor atroom temperature. Subsequently, a hydrogenation reaction -was conductedat 220° C. for 3 hours. The reaction pressure at 220° C. was 13 MPaG.After the reaction had been terminated, the temperature was reduced toroom temperature and the pressure was then reduced. An analysis of thereaction liquid by gas chromatography confirmed that the molar yield of10-decanol in the reaction was 76.5% and the molar ratio of theby-products (nonane and decane) to the target component (10-decanol) was0.004.

Example II-13

A 5% rhenium-5% germanium/zirconium oxide catalyst was prepared by thesame catalyst preparation method as in Example II-8, except thatzirconium oxide particles having a specific surface area of 97 m²/gwhich did not include a sulfate ion was used instead of the titaniumoxide particles. Subsequently, a hydrogenation reaction was conducted asin Example II-8, except that a water solvent was used instead ofmethanol. The molar yield of 10-decanol in the reaction was 23.2% andthe molar ratio of the by-products (nonane and decane) to the targetcomponent (10-decanol) was 0.001.

A comparison between the results obtained in Examples II-1, to II-3, andthe results obtained in Comparative examples II-1 to II-3, where acatalyst including a carrier composed of titanium oxide was used,confirms that using a catalyst including rhenium and a specific amountof second component increases the total amount of 1,10-decanediol and10-hydroxydecanoic acid produced in a hydrogenation reaction of acarboxylic acid per unit specific surface area and enhances catalyticactivity per unit specific surface area. Furthermore, the occurrence ofside reactions, such as a defunctionalization reaction associated withdehydration and hydrogenation, can be markedly reduced. The advantageouseffects become significant particularly when a catalyst includinggermanium is used. Note chat, the total amount of 1,10-decanediol and10-hydroxydecancic acid produced is used as a measure of catalyticactivity because 10-hydroxydecanoic acid is considered a reactionintermediate of the 1,10-decanediol product and can be derived into1,10-decanediol when the reaction times is further prolonged. Acomparison between the results obtained in Examples II-12 and II-13confirms that a catalyst including a carrier composed of zirconium oxidealso has the same advantageous effects as a catalyst, including acarrier composed of titanium oxide.

Specifically, it is confirmed that a catalyst including a zirconiumoxide carrier has a catalytic activity comparable to that of a catalystincluding a titanium oxide carrier in terms of catalytic activity perunit specific surface area. A comparison between the results obtained inExamples II-1 and II-2 confirms that reaction selectivity can bemaintained by using a catalyst that includes germanium even underhigh-inversion-rate reaction conditions, which have been an issue forrhenium catalysts. In addition, a comparison between the resultsobtained in Examples II-1, II-4, and II-5 confirms that the higher thesulfate ion content in the catalyst, the higher the degree of reductionin the defunctionalization reaction, the higher the reactionselectivity, and the higher the degree of increase in the catalyticactivity of the hydrogenation catalyst per unit specific surface area ofthe carrier. The remarkable reduction in the side reactions enables theproduction of an alcohol with a high purity and a reduction in the costsof purification of the alcohol produced.

INDUSTRIAL APPLICABILITY

This catalyst is industrially useful as a catalyst for directlysynthesizing an alcohol from a carbonyl compound. This catalyst enablesan intended alcohol to fee produced with high activity and highselectivity and reduces increases in the costs of purification of theproduct and the costs of production of the catalyst. Therefore, thiscatalyst is industrially highly valuable.

Although the present invention has been described in detail withreference to particular embodiments, it is apparent to a person skilledin the art that various modifications can be mace therein withoutdeparting from the spirit and scope of the present invention.

The present application is based on Japanese Patent Application No.2017-043988 filed on Mar. 8, 2017, and Japanese Patent Application No.2017-102053 filed on May 2 2017, which are incorporated herein byreference in their entirety.

1-26. (canceled)
 27. A method for producing a catalyst, the catalystcomprising a metal component comprising a first component that isrhenium and one or more second components selected from the groupconsisting of silicon, gallium, germanium, and indium, and a carrier onwhich the metal component is supported, the carrier comprising an oxideof a metal belonging to Group 4 of the periodic table, the methodcomprising: attaching the metal component the carrier to form ametal-supporting material; reducing the metal-supporting material with areducing gas to form a metal-supporting catalyst; and then oxidizing themetal-supporting catalyst.
 28. The method according to claim 27, whereinthe carrier comprises a sulfate ion, the content of the sulfate ion inthe carrier being 0.01% by mass to 10% by mass of the mass of thecarrier.
 29. A catalyst comprising a metal component comprising a firstcomponent that is rhenium and one or more second components selectedfrom the group consisting of silicon, gallium, germanium, and indium,and a carrier on which the metal component is supported, the carriercomprising an oxide of a metal belonging to Group 4 of the periodictable.
 30. The catalyst according to claim 29, wherein a mass ratio ofelements that are the second components to the rhenium element is in arange of 0.1 to
 10. 31. The catalyst according to claim 29, wherein theoxide of a metal belonging to Group 4 of the periodic table comprisestitanium oxide and/or zirconium oxide.
 32. The catalyst according toclaim 29, wherein the catalyst comprises a sulfate ion, and the sulfateion content in the catalyst is 0.01% by mass to 10% by mass of the massof the catalyst.
 33. The catalyst according to claim 29, wherein thecatalyst is suitable for hydrogenation of a carbonyl compound.
 34. Acatalyst comprising a metal component comprising a first component thatis rhenium and one or more second components selected from the groupconsisting of silicon, gallium, germanium, and indium, and a carrier onwhich the metal component is supported, the mass ratio of elements thatare the second components to the rhenium element being in a range of 0.1to
 10. 35. The catalyst according to claim 34, wherein the secondcomponents comprise germanium.
 36. The catalyst according to claim 34,wherein the metal component further comprises a third component which isa metallic element belonging to Groups 8 to 10 of the periodic table,the metallic element being other than iron or nickel, and wherein a massratio of the metallic element to an amount of the rhenium element isless than 0.2.
 37. The catalyst according to claim 36, wherein themetallic element comprises ruthenium.
 38. The catalyst according toclaim 34, wherein the carrier is a carbonaceous carrier or a carriercomprising an oxide of a metal belonging to Group 4 of the periodictable.
 39. The catalyst according to claim 34, wherein the catalystcomprises a sulfate ion, and the sulfate ion content in the catalyst is0.01% by mass to 10% by mass.
 40. The catalyst according to claim 34,wherein the catalyst is suitable for hydrogenation of a carbonylcompound.